U.S. patent number 10,286,335 [Application Number 14/485,606] was granted by the patent office on 2019-05-14 for systems including a condensing apparatus such as a bubble column condenser.
This patent grant is currently assigned to Gradiant Corporation. The grantee listed for this patent is Gradiant Corporation. Invention is credited to Prakash Narayan Govindan, Steven Lam, Maximus G. St. John.
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United States Patent |
10,286,335 |
Govindan , et al. |
May 14, 2019 |
Systems including a condensing apparatus such as a bubble column
condenser
Abstract
Condensing apparatuses and their use in various heat and mass
exchange systems are generally described. The condensing
apparatuses, such as bubble column condensers, may employ a heat
exchanger positioned external to the condensing vessel to remove
heat from a bubble column condenser outlet stream to produce a heat
exchanger outlet stream. In certain cases, the condensing apparatus
may also include a cooling device positioned external to the vessel
configured and positioned to remove heat from the heat exchanger
outlet stream to produce a cooling device outlet stream. The
condensing apparatus may be configured to include various internal
features, such as a vapor distribution region and/or a plurality of
liquid flow control weirs and/or chambers within the apparatus
having an aspect ratio of at least 1.5. A condensing apparatus may
be coupled with a humidifier to form part of a desalination system,
in certain cases.
Inventors: |
Govindan; Prakash Narayan
(Melrose, MA), Lam; Steven (Medford, MA), St. John;
Maximus G. (Boston, MA) |
Applicant: |
Name |
City |
State |
Country |
Type |
Gradiant Corporation |
Woburn |
MA |
US |
|
|
Assignee: |
Gradiant Corporation (Woburn,
MA)
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Family
ID: |
51626166 |
Appl.
No.: |
14/485,606 |
Filed: |
September 12, 2014 |
Prior Publication Data
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Document
Identifier |
Publication Date |
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US 20150129410 A1 |
May 14, 2015 |
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Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
Issue Date |
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61907629 |
Nov 22, 2013 |
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61901757 |
Nov 8, 2013 |
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61877032 |
Sep 12, 2013 |
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Current U.S.
Class: |
1/1 |
Current CPC
Class: |
F24F
6/12 (20130101); B01F 3/04106 (20130101); B01D
5/003 (20130101); C02F 1/048 (20130101); B01F
3/04078 (20130101); B01D 5/0003 (20130101); B01D
1/14 (20130101); B01F 3/04 (20130101); B01D
3/225 (20130101); B01D 5/0075 (20130101); B01D
5/006 (20130101); C02F 1/04 (20130101); C02F
2103/08 (20130101); Y02A 20/124 (20180101); Y02W
10/37 (20150501) |
Current International
Class: |
B01D
5/00 (20060101); F24F 6/12 (20060101); B01D
1/14 (20060101); B01D 3/22 (20060101); C02F
1/04 (20060101); B01F 3/04 (20060101) |
References Cited
[Referenced By]
U.S. Patent Documents
Foreign Patent Documents
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1791557 |
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101538070 |
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DE |
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EP |
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FR |
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GB |
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Jun 1971 |
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GB |
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JP |
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JP |
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JP |
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S55-9508 |
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JP |
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H3-54703 |
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May 1991 |
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JP |
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2006-312134 |
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Nov 2006 |
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JP |
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2239460 |
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Oct 2004 |
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RU |
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WO 2005/075045 |
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WO |
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WO 2009/103112 |
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WO |
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WO 2011/028853 |
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WO |
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WO 2011/137149 |
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Nov 2011 |
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WO |
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WO 2012/112808 |
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Aug 2012 |
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WO |
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WO 2013/037047 |
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Mar 2013 |
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WO |
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WO 2013/072709 |
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May 2013 |
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WO |
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WO 2013/150040 |
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Oct 2013 |
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WO |
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WO 2014/200829 |
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Dec 2014 |
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WO |
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WO 2017/030941 |
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Feb 2017 |
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WO |
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Primary Examiner: Hobson; Stephen
Attorney, Agent or Firm: Wolf, Greenfield & Sacks,
P.C.
Parent Case Text
RELATED APPLICATIONS
This application claims priority under 35 U.S.C. .sctn. 119(e) to
U.S. Provisional Patent Application Ser. No. 61/877,032, filed Sep.
12, 2013, and entitled "Systems Including a Bubble Column
Condenser"; U.S. Provisional Patent Application Ser. No.
61/901,757, filed Nov. 8, 2013, and entitled "Systems Including a
Bubble Column Condenser"; and U.S. Provisional Patent Application
Ser. No. 61/907,629, filed Nov. 22, 2013, and entitled "Systems
Including a Bubble Column Condenser"; each of which is incorporated
herein by reference in its entirety for all purposes.
Claims
What is claimed is:
1. A humidifier system, comprising: a humidifier apparatus,
comprising: a vessel comprising a liquid inlet in fluid
communication with a source of a liquid comprising a condensable
fluid in liquid phase, a liquid outlet, and at least one chamber in
fluid communication with the liquid inlet and the liquid outlet,
wherein the at least one chamber comprises a bottom surface
comprising a plurality of perforations through which vapor can
travel; a liquid layer positioned in contact with the liquid
outlet, wherein the liquid layer comprises an amount of the liquid
comprising the condensable fluid in liquid phase; a vapor
distribution region positioned below the at least one chamber, the
vapor distribution region comprising a vapor inlet in fluid
communication with a source of a vapor mixture comprising the
condensable fluid in vapor phase and/or a non-condensable gas; and
a vapor outlet arranged in fluid communication with the at least
one chamber; and a liquid-to-liquid heat exchanger positioned
external to the vessel and fluidly connected to the liquid inlet
and the liquid outlet of the vessel, wherein the heat exchanger
receives and delivers heat to the liquid comprising the condensable
fluid in liquid phase prior to entry of the liquid comprising the
condensable fluid in liquid phase into the liquid inlet of the
vessel, wherein: the humidifier apparatus produces a
vapor-containing humidifier gas outlet stream enriched in the
condensable fluid in vapor phase relative to the vapor mixture
received from the vapor inlet, and the vapor-containing humidifier
gas outlet stream exits the vessel through the vapor outlet, and
the humidifier apparatus produces a liquid-containing stream
containing an amount of the condensable fluid in liquid phase, the
liquid-containing stream exits the vessel through the liquid
outlet, and at least a portion of the liquid-containing stream that
exits the vessel through the liquid outlet flows through the
liquid-to-liquid heat exchanger and is returned to the vessel
through the liquid inlet.
2. The humidifier system of claim 1, wherein the condensable fluid
comprises water.
3. The humidifier system of claim 1, wherein the vapor mixture
comprises air.
4. The humidifier system of claim 1, wherein the humidifier
apparatus further comprises a second vapor distribution region
comprising a vapor inlet in fluid communication with a source of a
vapor mixture comprising the condensable fluid in vapor phase
and/or a non-condensable gas.
5. The humidifier system of claim 1, wherein the at least one
chamber has an aspect ratio of at least about 1.5.
6. The humidifier system of claim 1, wherein the humidifier
apparatus has a substantially rectangular cross section.
7. The humidifier system of claim 1, wherein the humidifier
apparatus has a substantially parallelepiped shape.
8. The humidifier system of claim 1, wherein the at least one
chamber comprises a first weir and a second weir positioned along a
bottom surface of the chamber, wherein the first weir and second
weir each have a height that is less than the height of the
chamber, the first and second weirs being arranged such that a
stream of the liquid comprising the condensable fluid in liquid
phase flows across the chamber from the first weir to the second
weir.
9. The humidifier system of claim 8, wherein at least one of the
first and second weirs has a height of about 0.08 m or less.
10. The humidifier system of claim 1, wherein the at least one
chamber comprises at least one longitudinal baffle positioned along
a bottom surface of the chamber.
11. The humidifier system of claim 1, wherein the humidifier
apparatus further comprises a first chamber and a second chamber
arranged in a vertical manner with respect to one another and in
fluid communication with the liquid inlet and the liquid outlet,
wherein the first and second chambers are arranged such that the
liquid comprising the condensable fluid in liquid phase flows
across the length of the first chamber in a first direction and
across the length of the second chamber in a second, opposing
direction.
12. A humidifier apparatus, comprising: a vessel comprising: a
liquid inlet in fluid communication with a source of a liquid
comprising a condensable fluid in liquid phase; a liquid outlet;
and at least one chamber in fluid communication with the liquid
inlet and the liquid outlet, the at least one chamber comprising: a
bottom surface comprising a plurality of perforations through which
vapor can travel; and a first weir and a second weir positioned
along the bottom surface of the chamber, wherein the first weir and
second weir each have a height that is less than the height of the
chamber, and are arranged such that a stream of the liquid
comprising the condensable fluid in liquid phase flows across the
chamber from the first weir to the second weir, and wherein the
second weir has a height of about 0.08 m or less; a liquid layer
positioned in contact with the liquid outlet, wherein the liquid
layer comprises an amount of the liquid comprising the condensable
fluid in liquid phase; a vapor distribution region positioned below
the at least one chamber, the vapor distribution region comprising
a vapor inlet in fluid communication with a source of a vapor
mixture comprising the condensable fluid in vapor phase and/or a
non-condensable gas; and a vapor outlet arranged in fluid
communication with the at least one chamber, wherein: the
humidifier apparatus produces a vapor-containing humidifier gas
outlet stream enriched in the condensable fluid in vapor phase
relative to the vapor mixture received from the vapor inlet, and
the vapor-containing humidifier gas outlet stream exits the vessel
through the vapor outlet, and the humidifier apparatus produces a
liquid-containing stream containing an amount of the condensable
fluid in liquid phase, the liquid-containing stream exits the
vessel through the liquid outlet, and at least a portion of the
liquid-containing stream that exits the vessel through the liquid
outlet is returned to the vessel through the liquid inlet.
13. The humidifier apparatus of claim 12, wherein the condensable
fluid comprises water.
14. The humidifier apparatus of claim 12, wherein the vapor mixture
comprises air.
15. The humidifier apparatus claim 12, further comprising a second
vapor distribution region comprising a vapor inlet in fluid
communication with a source of a vapor mixture comprising the
condensable fluid in vapor phase and/or a non-condensable gas.
16. The humidifier apparatus of claim 12, wherein the at least one
chamber has an aspect ratio of at least about 1.5.
17. The humidifier apparatus of claim 12, wherein the humidifier
apparatus has a substantially rectangular cross section.
18. The humidifier apparatus of claim 12, wherein the humidifier
apparatus has a substantially parallelepiped shape.
19. The humidifier apparatus of claim 12, wherein the at least one
chamber comprises at least one longitudinal baffle positioned along
a bottom surface of the chamber.
20. The humidifier apparatus of claim 12, further comprising a
first chamber and a second chamber arranged in a vertical manner
with respect to one another and in fluid communication with the
liquid inlet and the liquid outlet, wherein the first and second
chambers are arranged such that the liquid comprising the
condensable fluid in liquid phase flows across the length of the
first chamber in a first direction and across the length of the
second chamber in a second, opposing direction.
Description
FIELD
Embodiments described herein generally relate to condensing
apparatuses (e.g., bubble column condensers) and their use in
various heat and mass exchange systems.
BACKGROUND
Fresh water shortages are becoming an increasing problem around the
world, as demand for fresh water for human consumption, irrigation,
and/or industrial use continues to grow. Various desalination
methods are capable of producing fresh water from seawater,
brackish water, flowback water, water produced from an oil or gas
extraction process, and/or waste water. For example, a
humidification-dehumidification (HDH) process involves contacting a
saline solution with dry air in a humidifier, such that the air
becomes heated and humidified. The heated and humidified air is
then brought into contact with cold water in a dehumidifier (e.g.,
condenser), producing pure water and dehumidified air.
However, HDH processes often involve certain drawbacks. For
example, due to the use of a carrier gas in HDH systems, a large
percentage of non-condensable gas (e.g., air) is generally present
in the condensing streams, which can cause heat and mass transfer
rates in the dehumidifier to be very low. Also, the presence of a
non-condensable gas can increase the thermal resistance to
condensation of vapor on a cold surface, thereby reducing the
effectiveness of surface condensers. Additionally, the dehumidifier
can sometimes require large amounts of energy to operate.
Condensers with improved properties, such as, for example, reduced
power consumption and/or high heat and mass transfer rates in the
presence of non-condensable gases, are therefore desirable.
SUMMARY
Condensing apparatuses, such as bubble column condensers, and their
use in various heat and mass exchange systems are disclosed. The
subject matter of the present invention involves, in some cases,
interrelated products, alternative solutions to a particular
problem, and/or a plurality of different uses of one or more
systems and/or articles.
Certain embodiments relate to desalination systems. In some
embodiments, a desalination system comprises a humidifier
comprising a humidifier liquid inlet fluidically connected to a
source of salt-containing water, a humidifier gas inlet fluidically
connected to a source of a carrier gas, and a humidifier outlet. In
certain cases, the humidifier is configured to produce a
vapor-containing humidifier outlet stream enriched in water vapor
relative to the gas received from the gas inlet. In some
embodiments, the desalination system comprises a bubble column
condenser comprising a condenser inlet fluidically connected to the
humidifier outlet, a condenser gas outlet, and a condenser water
outlet. In certain embodiments, the bubble column condenser is
configured to remove at least a portion of the water vapor from the
humidifier outlet stream to produce a condenser gas outlet stream
lean in water relative to the humidifier outlet stream and a
condenser water outlet stream. In some embodiments, the
desalination system comprises a heat exchanger separate from the
bubble column condenser and fluidically connected to the condenser
water outlet and configured to remove heat from the condenser water
outlet stream.
In some embodiments, the desalination system comprises a humidifier
comprising a humidifier liquid inlet fluidically connected to a
source of salt-containing water, a humidifier gas inlet fluidically
connected to a source of a gas, and a humidifier outlet, wherein
the humidifier is configured to produce a vapor-containing
humidifier outlet stream enriched in water vapor relative to the
gas received from the gas inlet. In certain embodiments, the
desalination system comprises a bubble column condenser comprising
a condenser inlet fluidically connected to the humidifier outlet, a
condenser gas outlet, and a condenser water outlet, wherein the
bubble column condenser is configured to remove at least a portion
of the water vapor from the humidifier outlet stream to produce a
condenser gas outlet stream lean in water relative to the
humidifier outlet stream and a condenser water outlet stream. In
some embodiments, the desalination system comprises a heat
exchanger fluidically connected to the condenser water outlet and
configured to remove heat from the condenser water outlet stream.
In certain cases, a portion of a gas flow is extracted from at
least one intermediate location in the humidifier and fed from each
of said at least one intermediate location to a corresponding
intermediate location in the bubble column condenser.
Certain embodiments relate to condenser systems comprising a bubble
column condenser comprising a vessel comprising an inlet in fluid
communication with a source of a gas comprising a condensable fluid
in vapor phase, and an outlet, wherein the vessel contains a liquid
layer comprising an amount of the condensable fluid and the bubble
column condenser is configured to remove at least a portion of the
condensable fluid from the gas to produce a bubble column condenser
outlet stream comprising the condensable fluid in liquid phase. In
some embodiments, the condenser systems further comprise a heat
exchanger positioned external to the vessel and fluidically
connected to the vessel to receive the bubble column condenser
outlet stream and to remove heat from the bubble column condenser
outlet stream.
Some embodiments relate to a bubble column condenser comprising a
first stage comprising a first stage inlet in fluid communication
with a source of a gas comprising a condensable fluid in a vapor
phase, and a first stage outlet, wherein the first stage contains a
liquid layer comprising an amount of the condensable fluid, and the
ratio of the height of the liquid layer within the first stage to
the length of the condenser is about 1.0 or lower during
substantially continuous operation.
In certain embodiments, the bubble column condenser comprises a
first stage comprising a first stage inlet in fluid communication
with a source of a gas comprising a condensable fluid in a vapor
phase, and a first stage outlet, wherein the first stage contains a
liquid layer comprising an amount of the condensable fluid, the
liquid layer having a height of less than about 0.1 m during
substantially continuous operation.
In some embodiments, a condenser apparatus is provided. In some
cases, the condenser apparatus comprises a vessel comprising a
liquid inlet for receiving a stream of a liquid comprising a
condensable fluid in liquid phase, a liquid outlet, and at least
one chamber in fluid communication with the liquid inlet and the
liquid outlet. In certain embodiments, the at least one chamber
comprises a bottom surface comprising a plurality of perforations
through which vapor can travel. In certain cases, the condenser
apparatus comprises a liquid layer positioned in contact with the
liquid outlet. In some cases, the liquid layer comprises an amount
of the liquid comprising the condensable fluid. In some
embodiments, the condenser apparatus comprises a vapor distribution
region positioned below the at least one chamber. According to some
embodiments, the vapor distribution region comprises a vapor inlet
in fluid communication with a source of a vapor mixture comprising
the condensable fluid in vapor phase and/or a non-condensable gas.
In some cases, the condenser apparatus comprises a vapor outlet
arranged in fluid communication with the at least one chamber. In
certain embodiments, the condenser apparatus is configured to
remove at least a portion of the condensable fluid from the vapor
mixture to produce a condenser outlet stream comprising the
condensable fluid in liquid phase.
In some embodiments, a humidifier apparatus is provided. In some
cases, the humidifier apparatus comprises a vessel comprising a
liquid inlet for receiving a stream of a liquid comprising a
condensable fluid in liquid phase, a liquid outlet, and at least
one chamber in fluid communication with the liquid inlet and the
liquid outlet. In certain embodiments, the at least one chamber
comprises a bottom surface comprising a plurality of perforations
through which vapor can travel. In certain cases, the humidifier
apparatus comprises a liquid layer positioned in contact with the
liquid outlet. In some cases, the liquid layer comprises an amount
of the liquid comprising the condensable fluid. In some
embodiments, the humidifier apparatus comprises a vapor
distribution region positioned below the at least one chamber.
According to some embodiments, the vapor distribution region
comprises a vapor inlet in fluid communication with a source of a
vapor mixture comprising the condensable fluid in vapor phase
and/or a non-condensable gas. In some cases, the humidifier
apparatus comprises a vapor outlet arranged in fluid communication
with the at least one chamber. In certain embodiments, the
humidifier apparatus is configured to produce a vapor-containing
humidifier outlet stream enriched in the condensable fluid in vapor
phase relative to the vapor mixture received from the vapor
inlet.
Some embodiments relate to a condenser apparatus comprising a
vessel comprising a liquid inlet for receiving a stream of a liquid
comprising a condensable fluid in liquid phase, a liquid outlet,
and at least one chamber in fluid communication with the liquid
inlet and the liquid outlet. In some cases, the at least one
chamber has an aspect ratio of at least 1.5. In some embodiments,
the condenser apparatus comprises a vapor inlet arranged in fluid
communication with the at least one chamber and with a source of a
vapor mixture comprising the condensable fluid in vapor phase
and/or a non-condensable gas. In some embodiments, the condenser
apparatus comprises a vapor outlet arranged in fluid communication
with the at least one chamber. In certain cases, the at least one
chamber comprises a surface comprising a plurality of perforations
through which vapor can travel. In some embodiments, the at least
one chamber comprises a first weir and a second weir, each
positioned along a bottom surface of the at least one chamber and
each having a height that is less than the height of the at least
one chamber. In certain embodiments, the first weir and second weir
are arranged such that the stream of the liquid comprising the
condensable fluid in liquid phase flows across the at least one
chamber from the first weir to the second weir. In certain
embodiments, the condenser apparatus is configured to remove at
least a portion of the condensable fluid from the vapor mixture to
produce a condenser outlet stream comprising the condensable fluid
in liquid phase.
According to some embodiments, a humidifier apparatus comprises a
vessel comprising a liquid inlet for receiving a stream of a liquid
comprising a condensable fluid in liquid phase, a liquid outlet,
and at least one chamber in fluid communication with the liquid
inlet and the liquid outlet. In some cases, the at least one
chamber has an aspect ratio of at least 1.5. In some embodiments,
the humidifier apparatus comprises a vapor inlet arranged in fluid
communication with the at least one chamber and with a source of a
vapor mixture comprising the condensable fluid in vapor phase
and/or a non-condensable gas. In some embodiments, the humidifier
apparatus comprises a vapor outlet arranged in fluid communication
with the at least one chamber. In certain cases, the at least one
chamber comprises a surface comprising a plurality of perforations
through which vapor can travel. In some embodiments, the at least
one chamber comprises a first weir and a second weir, each
positioned along a bottom surface of the at least one chamber and
each having a height that is less than the height of the at least
one chamber. In certain embodiments, the first weir and second weir
are arranged such that the stream of the liquid comprising the
condensable fluid in liquid phase flows across the at least one
chamber from the first weir to the second weir. In certain
embodiments, the humidifier apparatus is configured to produce a
vapor-containing humidifier outlet stream enriched in the
condensable fluid in vapor phase relative to the vapor mixture
received from the vapor inlet.
Certain embodiments relate to a condenser apparatus comprising a
vessel comprising a liquid inlet for receiving a stream of a liquid
comprising a condensable fluid in liquid phase, a liquid outlet,
and a plurality of chambers arranged in a vertical manner with
respect to one another and in fluid communication with the liquid
inlet and the liquid outlet. In some embodiments, the plurality of
chambers comprises a first chamber comprising a top surface
arranged in fluid communication with the liquid inlet and a bottom
surface comprising a plurality of perforations through which vapor
can travel. In some embodiments, the plurality of chambers further
comprises a second chamber arranged below the first chamber and in
fluid communication with the first chamber. In certain cases, the
second chamber comprises a plurality of perforations through which
vapor can travel. In some embodiments, the condenser apparatus
comprises a vapor inlet arranged in fluid communication with the
plurality of chambers and with a source of a vapor mixture
comprising a condensable fluid in vapor phase and/or a
non-condensable gas. In some cases, the condenser apparatus
comprises a vapor outlet arranged in fluid communication with the
plurality of chambers. In certain embodiments, the first and second
chambers are arranged such that the stream of the liquid comprising
the condensable fluid in liquid phase flows across the length of
the first chamber in a first direction and across the length of the
second chamber in a second, opposing direction. In certain
embodiments, the condenser apparatus is configured to remove at
least a portion of the condensable fluid from the vapor mixture to
produce a condenser outlet stream comprising the condensable fluid
in liquid phase.
In some embodiments, a humidifier apparatus comprises a vessel
comprising a liquid inlet for receiving a stream of a liquid
comprising a condensable fluid in liquid phase, a liquid outlet,
and a plurality of chambers arranged in a vertical manner with
respect to one another and in fluid communication with the liquid
inlet and the liquid outlet. In some embodiments, the plurality of
chambers comprises a first chamber comprising a top surface
arranged in fluid communication with the liquid inlet and a bottom
surface comprising a plurality of perforations through which vapor
can travel. In some embodiments, the plurality of chambers further
comprises a second chamber arranged below the first chamber and in
fluid communication with the first chamber. In certain cases, the
second chamber comprises a plurality of perforations through which
vapor can travel. In some embodiments, the humidifier apparatus
comprises a vapor inlet arranged in fluid communication with the
plurality of chambers and with a source of a vapor mixture
comprising a condensable fluid in vapor phase and/or a
non-condensable gas. In some cases, the humidifier apparatus
comprises a vapor outlet arranged in fluid communication with the
plurality of chambers. In certain embodiments, the first and second
chambers are arranged such that the stream of the liquid comprising
the condensable fluid in liquid phase flows across the length of
the first chamber in a first direction and across the length of the
second chamber in a second, opposing direction. In certain
embodiments, the humidifier apparatus is configured to produce a
vapor-containing humidifier outlet stream enriched in the
condensable fluid in vapor phase relative to the vapor mixture
received from the vapor inlet.
In some embodiments, a condenser apparatus is provided comprising a
vessel comprising a liquid inlet for receiving a stream of a liquid
comprising a condensable fluid in liquid phase, a liquid outlet,
and a plurality of chambers arranged in a vertical manner with
respect to one another and in fluid communication with the liquid
inlet and the liquid outlet. In certain cases, each chamber has an
aspect ratio of at least 1.5. In some embodiments, the plurality of
chambers comprises a first chamber comprising a top surface
arranged in fluid communication with the liquid inlet and a bottom
surface comprising a plurality of perforations through which vapor
can travel, and a second chamber arranged below the first chamber
and in fluid communication with the first chamber, the second
chamber comprising a plurality of perforations through which vapor
can travel. In some embodiments, the condenser apparatus comprises
a liquid layer positioned in contact with the liquid outlet. In
certain cases, the liquid layer comprises an amount of the liquid
comprising the condensable fluid. In certain embodiments, the
condenser apparatus comprises a vapor distribution region
positioned below the plurality of chambers. In some cases, the
vapor distribution region comprises a vapor inlet in fluid
communication with a source of a vapor mixture comprising a
condensable fluid in vapor phase and/or a non-condensable gas. In
some embodiments, the condenser apparatus comprises a vapor outlet
arranged in fluid communication with the plurality of chambers. In
some embodiments, each of the first chamber and the second chamber
comprises a first weir and a second weir positioned along a bottom
surface of the first or second chamber. In some cases, the first
weir and second weir each have a height that is less than the
height of the first or second chamber. In some cases, the first and
second weirs are arranged such that the stream of the liquid
comprising the condensable fluid in liquid phase flows across the
chamber from the first weir to the second weir. In some
embodiments, the first and second chambers are arranged such that
the stream of the liquid comprising the condensable fluid in liquid
phase flows across the length of the first chamber in a first
direction and across the length of the second chamber in a second,
opposing direction. In certain embodiments, the condenser apparatus
is configured to remove at least a portion of the condensable fluid
from the vapor mixture to produce a condenser outlet stream
comprising the condensable fluid in liquid phase.
In some embodiments, a humidifier apparatus is provided comprising
a vessel comprising a liquid inlet for receiving a stream of a
liquid comprising a condensable fluid in liquid phase, a liquid
outlet, and a plurality of chambers arranged in a vertical manner
with respect to one another and in fluid communication with the
liquid inlet and the liquid outlet. In certain cases, each chamber
has an aspect ratio of at least 1.5. In some embodiments, the
plurality of chambers comprises a first chamber comprising a top
surface arranged in fluid communication with the liquid inlet and a
bottom surface comprising a plurality of perforations through which
vapor can travel, and a second chamber arranged below the first
chamber and in fluid communication with the first chamber, the
second chamber comprising a plurality of perforations through which
vapor can travel. In some embodiments, the humidifier apparatus
comprises a liquid layer positioned in contact with the liquid
outlet. In certain cases, the liquid layer comprises an amount of
the liquid comprising the condensable fluid. In certain
embodiments, the humidifier apparatus comprises a vapor
distribution region positioned below the plurality of chambers. In
some cases, the vapor distribution region comprises a vapor inlet
in fluid communication with a source of a vapor mixture comprising
a condensable fluid in vapor phase and/or a non-condensable gas. In
some embodiments, the humidifier apparatus comprises a vapor outlet
arranged in fluid communication with the plurality of chambers. In
some embodiments, each of the first chamber and the second chamber
comprises a first weir and a second weir positioned along a bottom
surface of the first or second chamber. In some cases, the first
weir and second weir each have a height that is less than the
height of the first or second chamber. In some cases, the first and
second weirs are arranged such that the stream of the liquid
comprising the condensable fluid in liquid phase flows across the
chamber from the first weir to the second weir. In some
embodiments, the first and second chambers are arranged such that
the stream of the liquid comprising the condensable fluid in liquid
phase flows across the length of the first chamber in a first
direction and across the length of the second chamber in a second,
opposing direction. In certain embodiments, the humidifier
apparatus is configured to produce a vapor-containing humidifier
outlet stream enriched in the condensable fluid in vapor phase
relative to the vapor mixture received from the vapor inlet.
Other advantages and novel features of the present invention will
become apparent from the following detailed description of various
non-limiting embodiments of the invention when considered in
conjunction with the accompanying figures. In cases where the
present specification and a document incorporated by reference
include conflicting and/or inconsistent disclosure, the present
specification shall control. If two or more documents incorporated
by reference include conflicting and/or inconsistent disclosure
with respect to each other, then the document having the later
effective date shall control.
BRIEF DESCRIPTION OF THE DRAWINGS
Non-limiting embodiments of the present invention will be described
by way of example with reference to the accompanying figures, which
are schematic and are not intended to be drawn to scale. In the
figures, each identical or nearly identical component illustrated
is typically represented by a single numeral. For purposes of
clarity, not every component is labeled in every figure, nor is
every component of each embodiment of the invention shown where
illustration is not necessary to allow those of ordinary skill in
the art to understand the invention. In the figures:
FIG. 1A shows, according to some embodiments, an exemplary
cross-sectional schematic illustration of a single-stage bubble
column condenser;
FIG. 1B shows, according to some embodiments, an exemplary top-down
view of a stage of a bubble column condenser;
FIG. 2A shows an exemplary cross-sectional schematic illustration
of a two-stage bubble column condenser without an intermediate gas
inlet, according to some embodiments;
FIG. 2B shows an exemplary cross-sectional schematic illustration
of a two-stage bubble column condenser with an intermediate gas
inlet, according to some embodiments;
FIG. 2C shows an exemplary cross-sectional schematic illustration
of a two-stage bubble column condenser with a vapor distribution
chamber, according to some embodiments;
FIG. 2D shows an exemplary cross-sectional schematic illustration
of a two-stage bubble column condenser with a vapor distribution
chamber and an intermediate gas inlet, according to some
embodiments;
FIG. 3A shows, according to some embodiments, an exemplary
schematic diagram of a bubble column condenser and an external heat
exchanger;
FIG. 3B shows, according to some embodiments, an exemplary
schematic diagram of a bubble column condenser, an external heat
exchanger, an external heating device, and an external cooling
device;
FIG. 4A shows an exemplary schematic diagram of an HDH system
including a bubble column condenser and an external heat exchanger,
according to some embodiments, where the external heat exchanger is
a parallel flow device;
FIG. 4B shows, according to some embodiments, an exemplary
schematic diagram of an HDH system including a bubble column
condenser and an external heat exchanger, where the external heat
exchanger is a counter flow device;
FIG. 4C shows, according to some embodiments, an exemplary
schematic diagram of an HDH system including a bubble column
condenser, an external heat exchanger, a first external heating
device, and a second external heating device;
FIG. 5 shows an exemplary schematic diagram of an eight-stage
bubble column condenser and an external heat exchanger, according
to some embodiments;
FIG. 6 shows an exemplary embodiment of a baffled bubble-generating
chamber with two passes of liquid cross flow;
FIG. 7A shows an exemplary embodiment of a multi-stage bubble
column condenser in closed isometric view;
FIG. 7B shows a cross-sectional isometric view of the exemplary
embodiment of a multi-stage bubble column condenser shown in FIG.
7A;
FIGS. 7C-F show two-dimensional side-view or top-view projections
of the exemplary embodiment of a multi-stage bubble column
condenser shown in FIG. 7A;
FIG. 7G shows various views of the top surface of the exemplary
embodiment of a multi-stage bubble column condenser shown in FIG.
7A;
FIG. 7H shows various views of a bubble-generating chamber with one
pass of liquid cross flow in the exemplary embodiment of a
multi-stage bubble column condenser shown in FIG. 7A;
FIG. 7I shows a top-down view of a portion of a bubble-generating
chamber in the exemplary embodiment of a multi-stage bubble column
condenser shown in FIG. 7A;
FIG. 8 shows an exemplary cross-sectional schematic illustration of
a single-stage bubble column condenser comprising a stack to reduce
or eliminate droplet entrainment, according to some
embodiments;
FIG. 9 shows, according to some embodiments, an exemplary schematic
diagram of an HDH system including a bubble column condenser, a
heat exchanger, a first heating device, a second heating device,
and a cooling device;
FIG. 10A shows, according to some embodiments, an exemplary
schematic illustration of an eight-stage bubble column condenser
and an external heat exchanger;
FIG. 10B shows, according to some embodiments, an exemplary
schematic illustration of an eight-stage bubble column condenser,
an external heat exchanger, and an external cooling device;
FIG. 11A shows, according to some embodiments, an exemplary
schematic illustration of an HDH system comprising a bubble column
condenser, a humidifier, an external heat exchanger, an external
heating device, and an external cooling device;
FIG. 11B shows, according to some embodiments, an exemplary
schematic illustration of an HDH system comprising a bubble column
condenser comprising an intermediate air inlet, a humidifier
comprising an intermediate air outlet, an external heat exchanger,
an external heating device, and an external cooling device;
FIG. 11C shows, according to some embodiments, an exemplary
schematic illustration of an HDH system comprising a bubble column
condenser comprising an internal heat exchanger, a humidifier, an
external heating device, and an external cooling device;
FIG. 11D shows, according to some embodiments, an exemplary
schematic illustration of an HDH system comprising a bubble column
condenser comprising an internal heat exchanger and an intermediate
air inlet, a humidifier comprising an intermediate air outlet, an
external heating device, and an external cooling device;
FIG. 12 shows, according to some embodiments, an exemplary
schematic illustration of a chamber having a substantially circular
cross section and comprising a spiral baffle; and
FIG. 13 shows an exemplary schematic illustration of a chamber
having a substantially circular cross section and comprising two
baffles, according to some embodiments.
DETAILED DESCRIPTION
Embodiments described herein provide condensing apparatuses (e.g.,
bubble column condensers) and their use in various heat and mass
exchange systems. For example, the condensing apparatuses may be
useful in systems for purification of water (e.g., desalination
systems). In some cases, the condensing apparatuses allow for
simplified, lower cost systems with improved performance, such as
improved heat and mass exchange between gas and liquid phases. It
should be noted that while the apparatuses described herein are
generally referred to as condensing apparatuses or condensers, the
apparatuses may, in some cases, be used for humidification. For
example, certain of the embodiments described herein may relate to
bubble column humidifiers.
In some cases, the condensers may advantageously allow for a
reduced number of components, a reduced amount of material (e.g.,
heat transfer surface area) within a system, a reduced cost of
components, and/or components having reduced dimensions. For
example, a system may include a component containing an amount of a
liquid at a certain height, and incorporation of condensers
described herein may allow for a reduction in the amount, and,
hence, height, of the liquid within the component. In some cases,
reducing the amount of liquid within the system may allow for more
simplified components having reduced dimensions with similar or, in
some cases, improved performance relative to larger systems. For
example, a component may be useful in facilitating heat transfer
between gas and liquid phases within the condenser. Incorporation
of such components having reduced dimensions (e.g., height, stage
spacing, etc.) within a single condenser may allow for use of a
greater number of components within a given condenser, resulting in
increased heat and mass exchange between the gas and liquid phases.
Additionally, the amount of materials required to construct
condensers described herein may be reduced, thereby reducing cost
of fabrication. Further, in certain embodiments of the condensers
described herein, heat and mass transfer occurs through bubbles of
a gas or gas mixture (e.g., heat and mass may be transferred from
bubbles of a gas or gas mixture comprising a condensable fluid in
vapor phase to a liquid bath of the condensable fluid through a
condensation process). The use of gas bubbles rather than, for
example, metallic surfaces (e.g., titanium tubes) for heat and mass
transfer may advantageously reduce the fabrication cost of the
condensers. Further, the use of gas bubbles may increase the amount
of surface area available for heat and mass transfer, thereby
resulting in an advantageous increase in the thermodynamic
effectiveness of the bubble column condensers.
In some cases, condensers described herein may advantageously
exhibit a reduced pressure drop across the condenser. That is, the
pressure at an inlet of the condenser may be substantially the same
as (e.g., less than 10% variation from) the pressure at an outlet
of the condenser. For example, the pressure of a fluid (e.g.,
vapor) entering an inlet of the condenser may be substantially the
same as the pressure of the fluid exiting an outlet of the
condenser. Reduction of the pressure drop across the condenser may
be advantageous in that a relatively smaller pump, requiring less
power and cost to operate, may be used to pump fluids through the
condenser.
Condensers described herein may, in some embodiments, exhibit
improved heat transfer properties, a characteristic that may be
particularly advantageous in cases where the material passing
through the condenser includes a non-condensable gas.
Non-condensable gases generally refer to any gas that does not
condense into a liquid phase under the operating conditions of the
condenser. Examples of non-condensable gases include, but are not
limited to, air, nitrogen, oxygen, and helium. In some cases, the
condenser may be configured such that heat transfer rates are
improved for mixtures including a non-condensable gas.
Typically, the condenser may be configured to receive a condenser
liquid inlet stream and to deliver a condenser liquid outlet stream
to another component within a system. The condenser may also be
configured to receive a gas or gas mixture via at least one inlet
and to deliver a gas or gas mixture via an outlet to another
component within the system. In some embodiments, the gas or gas
mixture may comprise a vapor mixture (e.g., a condensable fluid in
vapor phase and/or a non-condensable gas). In some cases, the gas
or gas mixture entering the condenser may have a different
composition than the gas or gas mixture exiting the condenser. For
example, the gas or gas mixture entering the condenser may include
a particular fluid (e.g., a condensable fluid), a portion of which
may be removed in the condenser such that the exiting gas or gas
mixture has a relatively decreased amount of the fluid. In some
embodiments, the fluid may be removed from the gas or gas mixture
via a condensation process. In some cases, the condenser may be a
bubble column condenser, wherein vapors are condensed in a column
of relatively cold liquid. In some embodiments, the bubble column
condenser comprises at least one stage within which a gas or gas
mixture is treated such that one or more components of the gas or
gas mixture is removed. For example, the gas or gas mixture may
include a condensable fluid in vapor phase, and recovery of the
condensable fluid (e.g., in liquid form) may be performed within
the at least one stage of the bubble column condenser. A
condensable fluid generally refers to a fluid that is able to
condense from gas phase to liquid phase under the operating
conditions of the condenser.
FIG. 1A shows an exemplary cross-sectional diagram of a
single-stage bubble column condenser. As shown in FIG. 1A, bubble
column condenser 100 includes stage 110, which includes inlet 120,
outlet 130, and chamber 140 (e.g. as provided by a containing
vessel). Liquid layer 150, which comprises a condensable fluid in a
liquid phase, resides in chamber 140. As an illustrative
embodiment, the condensable fluid may be water. Liquid layer 150
may, in some embodiments, have a height H.sub.L that is relatively
low (e.g., about 0.1 m or less). Height H.sub.L may be less than a
height H.sub.C of chamber 140. In some cases, the portion of
chamber 140 that is not occupied by liquid layer 150 comprises a
vapor distribution region. Inlet 120 is in fluid communication with
a source of a gas or gas mixture containing a condensable fluid in
a vapor phase. In some embodiments, the gas may further contain one
or more non-condensable gases. For example, the gas may include
humidified air. Inlet 120 may also be coupled to bubble generator
160 such that gas entering inlet 120 is fed into bubble generator
160. As discussed in further detail below, the bubble generator may
comprise a sparger plate comprising a plurality of holes. Bubble
generator 160 may be in fluid communication with chamber 140 and/or
may be arranged within chamber 140. In some cases, bubble generator
160 forms the bottom surface of chamber 140.
In some cases, inlets and/or outlets within the column may be
provided as separate and distinct features (e.g., inlet 120 in FIG.
1A). In some cases, inlets and/or outlets within the column may be
provided by certain components such as the bubble generator,
sparger plate, and/or any other features which establish fluid
communication between components of the column and/or system. For
example, the "inlet" of a particular stage of the column may be
provided as the plurality of holes of a sparger plate. For example,
a gas or gas mixture travelling between a first and second stage
may enter the second stage via an "inlet" provided by holes of a
sparger plate.
When the bubble column condenser is in operation, the gas or gas
mixture flows through inlet 120 to bubble generator 160, producing
gas bubbles 170 that contain the gas or gas mixture and travel
through liquid bath (e.g., liquid layer) 150. The temperature of
liquid bath 150 may be maintained lower than the temperature of gas
bubbles 170, resulting in transfer of heat and mass from gas
bubbles 170 to liquid bath 150 through a condensation process.
After passing through liquid bath 150, the gas or gas mixture,
which has been at least partially dehumidified, may enter the vapor
distribution region (e.g., the portion of chamber 140 that is not
occupied by liquid bath 150). In some cases, the gas or gas mixture
may be substantially homogeneously distributed throughout the vapor
distribution region. The gas or gas mixture may then proceed to
exit the bubble column condenser through outlet 130. In an
exemplary embodiment, a gas mixture containing water and air may be
passed through bubble column condenser 100 such that gas bubbles
170 are formed containing both water in vapor form and air. Upon
contact with liquid bath 150, water may then be condensed and
transferred to liquid bath 150, thereby producing a dehumidified
gas that exits bubble column condenser 100 via outlet 130.
In some embodiments, the pressure of the gas or gas mixture at
inlet 120 is substantially the same as the pressure of the gas or
gas mixture at outlet 130. In some embodiments, the pressure of the
gas or gas mixture at inlet 120 differs from the pressure of the
gas or gas mixture at outlet 130 by about 1 kPa or less. In some
embodiments, the pressure of the gas or gas mixture at inlet 120 is
less than about 1 kPa larger than the pressure of the gas or gas
mixture at outlet 130.
As shown in FIG. 8, bubble column condenser 100 may further
comprise an optional stack 800 in fluid communication with outlet
130. Stack 800 may be added, for example, to reduce or eliminate
droplet entrainment (e.g., droplets of liquid from liquid bath 150
flowing out of outlet 130 with the dehumidified gas). In certain
embodiments, bubble column condenser 100 may comprise an optional
droplet eliminator (not shown in FIG. 8). The droplet eliminator
may, for example, comprise a mesh extending across the cross
section of bubble column condenser 100. In operation, entrained
liquid droplets may collide with the mesh and return to liquid bath
150. In some cases, reducing or eliminating droplet entrainment may
advantageously increase the amount of purified water recovered from
bubble column condenser 100 (e.g., by reducing the amount of
purified water that exits bubble column condenser 100 into the
ambient air). In certain embodiments, reducing or eliminating
droplet entrainment may increase the amount of purified water
recovered from bubble column condenser 100 by at least about 1%, at
least about 5%, at least about 10%, at least about 15%, at least
about 20%, at least about 30%, at least about 40%, at least about
50%, or at least about 60%. In some cases, reducing or eliminating
droplet entrainment may increase the amount of purified water
recovered from bubble condenser 100 by an amount in the range of
about 1% to about 10%, about 1% to about 20%, about 1% to about
40%, about 1% to about 60%, about 5% to about 20%, about 5% to
about 40%, about 5% to about 60%, about 10% to about 20%, about 10%
to about 30%, about 10% to about 40%, about 10% to about 50%, about
10% to about 60%, about 20% to about 30%, about 20% to about 40%,
about 20% to about 50%, about 20% to about 60%, about 30% to about
40%, about 30% to about 50%, about 30% to about 60%, about 40% to
about 50%, about 40% to about 60%, or about 50% to about 60%.
In some cases, stack 800 has a largest cross-sectional dimension
(e.g., length, diameter) D.sub.s that is greater than the largest
cross-sectional dimension D.sub.o of outlet 130. In certain
embodiments, largest cross-sectional dimension D.sub.s is at least
about 0.01 m, at least about 0.02 m, at least about 0.05 m, at
least about 0.1 m, at least about 0.2 m, at least about 0.5 m, at
least about 1 m, at least about 2 m, or at least about 5 m greater
than the largest cross-sectional dimension D.sub.o of outlet 130.
In some embodiments, largest cross-sectional dimension D.sub.s is
greater than largest cross-sectional dimension D.sub.o by an amount
in the range of about 0.01 m to about 0.05 m, about 0.01 m to about
0.1 m, about 0.01 m to about 0.5 m, about 0.01 m to about 1 m,
about 0.01 m to about 5 m, about 0.1 m to about 0.5 m, about 0.1 m
to about 1 m, about 0.1 m to about 5 m, about 0.5 m to about 1 m,
about 0.5 m to about 5 m, or about 1 m to about 5 m. Without
wishing to be bound by a particular theory, increasing the largest
cross-sectional dimension of a conduit through which the
dehumidified gas stream flows may reduce the velocity of the
dehumidified gas stream. As a result, any liquid droplets that may
be present in the dehumidified gas stream may fall out of the
dehumidified gas stream and return to liquid bath 150 instead of
exiting bubble column condenser 100 through outlet 130.
In some embodiments, the bubble column condenser comprises at least
two stages for recovery of a condensable fluid from a gas or gas
mixture. For example, the stages may be arranged such that a gas or
gas mixture flows sequentially from the first stage to the second
stage. In some cases, the stages may be arranged in a vertical
fashion, e.g., a first stage positioned below a second stage within
the condenser. In some cases, the stages may be arranged in a
horizontal fashion, e.g., a first stage positioned to the right of
a second stage. The presence of multiple stages within a bubble
column condenser may, in certain cases, advantageously lead to
higher recovery of the condensable fluid in liquid phase. For
example, the presence of multiple stages may provide numerous
locations wherein the gas or gas mixture may be treated to recover
the condensable fluid. That is, the gas or gas mixture may travel
through more than one liquid bath (e.g., liquid layer) in which at
least a portion of the gas or gas mixture undergoes condensation.
Additionally, in some embodiments, the use of multiple stages can
produce a condenser liquid outlet stream having increased
temperature (e.g., relative to the condenser liquid input stream),
as described more fully below. This may be advantageous in systems
where heat from the condenser liquid outlet stream is transferred
to a separate stream within the system, such as an
evaporator/humidifier input stream. In such cases, the ability to
produce a heated condenser liquid outlet stream can increase energy
effectiveness of the system. Additionally, use of multiple stages
may also enable greater flexibility for fluid flow within the
system. For example, extraction and/or injection of fluids from
intermediate bubble column stages may occur via intermediate
exchange conduits.
FIG. 2A shows an exemplary cross-sectional diagram of a multi-stage
bubble column condenser. In FIG. 2A, bubble column condenser 200
comprises first stage 210 and second stage 220 arranged vertically
above first stage 210. First stage 210 includes chamber 212, liquid
layer 214 positioned within chamber 212, and first inlet 234 for a
first gas or gas mixture comprising a condensable fluid in a vapor
phase. First stage 210 also includes a first vapor distribution
region, which is located above liquid layer 214 (e.g., the portion
of chamber 212 that is not occupied by liquid layer 214).
Additionally, first stage 210 comprises liquid outlet 216 for exit
of a condensed liquid output stream from condenser 200. First inlet
234, which is in fluid communication with a source of the first gas
or gas mixture, is also coupled to bubble generator 208 such that
the first gas or gas mixture entering inlet 234 is fed into bubble
generator 208. The first gas or gas mixture may be delivered to
inlet 234 by pump 202 through conduit 204 from a source of the
first gas or gas mixture fluidly connected to condenser 200. In
some embodiments, first gas inlet 234 and/or bubble generator 208
occupy the entire bottom surface of first stage 210 or chamber 212.
In other embodiments, first gas inlet 234 and/or bubble generator
208 occupy a smaller portion of the bottom surface of first stage
210 or chamber 212.
Second stage 220 is in fluid communication with first stage 210 and
includes chamber 224, liquid layer 226 positioned within chamber
224, and bubble generator 222, which is arranged to receive the
first gas or gas mixture from first stage 210. Second stage 220
also includes second stage liquid inlet 232, which is in fluid
communication with a source of the condensable fluid in liquid
phase and delivers the condensable fluid to liquid layer 226.
Additionally, second stage 220 comprises gas outlet 230, through
which a bubble column condenser gas outlet stream may exit. Second
stage 220 also comprises a second vapor distribution region located
above liquid layer 226 (e.g., the portion of chamber 224 that is
not occupied by liquid layer 226).
Conduit/downcomer 218 is positioned between first stage 210 and
second stage 220, providing a path for any overflowing condensable
fluid (e.g., from liquid layer 226) to travel from second stage 220
to liquid layer 214 in first stage 210. The maximum height of
liquid layer 226 is set by weir 228, such that any additional
condensable fluid of liquid layer 226 above that maximum height
flows through conduit/downcomer 218 to liquid layer 214 in first
stage 210. The outlet of conduit/downcomer 218 is submerged in
liquid layer 214, such the first gas or gas mixture flowing through
first stage 210 is prevented from entering conduit/downcomer 218.
In some cases, first stage 210 further comprises optional weir 254.
Optional weir 254 may establish a height of liquid surrounding
conduit/downcomer 218 that is higher than the height of liquid
layer 214 in first stage 210. It has been recognized that it may be
advantageous for the height of liquid surrounding conduit/downcomer
218 to be higher than the height of liquid layer 214, as such a
configuration may result in the hydrostatic head of liquid that the
first gas or gas mixture has to overcome being higher in the liquid
around conduit/downcomer 218 than in liquid layer 214. Such a
configuration may thus prevent the first gas or gas mixture from
flowing through conduit/downcomer 218 and thereby bypassing bubble
generator 222.
Optional vapor distribution chamber 206 may be positioned below
first stage 210 and may allow the first gas or gas mixture to be
distributed along the bottom surface of bubble generator 208. Those
of ordinary skill in the art would be capable of selecting the
appropriate system configuration for use in a particular
application.
In operation, a first gas or gas mixture (provided by a source of
gas not pictured in FIG. 2) containing a condensable fluid is
pumped by pump 202 through conduit 204 to optional vapor
distribution chamber 206, where the first gas or gas mixture is
substantially homogeneously distributed along the bottom surface of
first stage 210 to first stage gas inlet 234 and bubble generator
208. As the first gas or gas mixture travels through bubble
generator 208, gas bubbles are formed. The gas bubbles travel
through liquid layer 214, which is maintained at a temperature
below that of the gas bubbles. The gas bubbles undergo a
condensation process and transfer heat and/or mass of the
condensable fluid to liquid layer 214. For example, the condensable
fluid may be water, such that the gas bubbles are at least
partially dehumidified as they travel through liquid layer 214.
Bubbles of the at least partially dehumidified gas then enter the
first vapor distribution region. The at least partially
dehumidified gas may, in some cases, be substantially homogenously
distributed throughout the first vapor distribution region. The at
least partially dehumidified gas then enters bubble generator 222,
where gas bubbles of the at least partially dehumidified gas are
formed. Bubbles of the at least partially dehumidified gas then
travel through liquid layer 226, which is maintained at a
temperature below that of the gas bubbles, and heat and mass of the
condensable fluid are transferred to liquid layer 226. Bubbles of
the further dehumidified gas then enter the second vapor
distribution region. The further dehumidified gas may, in some
cases, be substantially homogeneously distributed throughout the
second vapor distribution region. The further dehumidified gas then
exits the bubble column condenser through second stage outlet 230
as a bubble column condenser gas outlet stream.
In some embodiments, a stream of condensable fluid in liquid phase
flows in the opposite direction as (i.e., counterflow to) the gas
or gas mixture. For example, condensable liquid can enter bubble
column condenser 200 through second stage liquid inlet 232, which
is in fluid communication with a source of the condensable fluid in
liquid phase. The condensable liquid is first delivered to liquid
layer 226, which has a maximum height specified by weir 228. If the
height of liquid layer 226 exceeds the maximum height, an amount of
condensable liquid may spill over the top of the weir through
conduit/downcomer 218 to liquid layer 214 and exit the condenser
via condenser liquid outlet 216. The temperature of the condenser
liquid outlet stream may be greater than that of the condensable
liquid entering the condenser at second stage liquid inlet 232, as
the condensable liquid is passed through various stages within the
condenser. In some cases, heat is transferred to the condensable
liquid at each of the stages within the bubble column condenser. In
some cases, as the number of stages through which the condensable
fluid passes increases, the temperature of the condenser liquid
outlet stream increases. Such a configuration may be advantageous
in systems where heat from the condenser liquid outlet stream is
transferred to another component within the system. In some cases,
the heat transfer may occur at a location within the system that is
not within the condenser. For example, heat from the condenser
liquid outlet stream may be transferred to a humidifier input
stream within a humidifier and/or a heat exchanger in fluid
communication with the condenser.
As shown in FIG. 2B, bubble condenser 200 can further comprise an
optional second inlet 205. Optional second inlet 205 may be in
fluid communication with a source of a second gas or gas mixture,
and the second gas or gas mixture may be delivered to inlet 205 via
optional conduit 203. The second gas or gas mixture may comprise a
condensable fluid in vapor phase. In certain cases, the condensable
fluid may be water. The second gas or gas mixture may, in some
embodiments, further comprise one or more non-condensable gases
(e.g., air).
In some embodiments, a bubble column condenser may comprise at
least one vapor distribution region to allow for introduction of a
vapor mixture that contains a condensable fluid in vapor phase
and/or a non-condensable gas (e.g., carrier gas). Typically, the
vapor distribution region may be selected to have sufficient volume
to allow vapors to substantially evenly diffuse over the cross
section of the bubble column condenser. In some cases, the vapor
distribution chamber may provide sufficient volume to allow
entrained droplets from a liquid layer in a stage to return to the
liquid layer. In some cases, the vapor distribution region may be
positioned at or near a bottom portion of the bubble column
condenser. In some cases, the vapor distribution region is
positioned between two consecutive or adjacent bubble generating
chambers. For example, the vapor distribution region may keep the
liquid layers of the two consecutive or adjacent bubble generating
chambers separate, thereby increasing the thermodynamic
effectiveness of the bubble column condenser. The vapor
distribution region may include a vapor inlet in fluid
communication with a source of a vapor mixture comprising a
condensable fluid in vapor phase and/or a non-condensable gas. In
some cases, the bubble column condenser includes more than one
vapor distribution region.
In some embodiments, a vapor distribution chamber comprising a
vapor distribution region may further comprise a liquid layer
(e.g., a sump volume). For example, liquid may collect in the sump
volume after exiting the last stage of a bubble column condenser,
prior to exiting the bubble column condenser. In some embodiments,
the sump volume may be in direct contact with a liquid outlet of
the bubble column condenser. In certain cases, the sump volume may
be in fluid communication with a pump that pumps liquid out of the
bubble column condenser. The sump volume may, for example, provide
a positive suction pressure on the intake of the pump, and may
advantageously prevent negative (e.g., vacuum) suction pressure
that may induce deleterious cavitation bubbles. In some cases, the
sump volume may advantageously decrease the sensitivity of the
bubble column condenser to sudden changes in heat transfer rates
(e.g., due to intermittent feeding of salt-containing water and/or
intermittent discharge of pure water).
FIG. 2C provides an exemplary illustration of a bubble column
condenser containing a vapor distribution region positioned above
an amount of a condensable fluid in liquid phase. In FIG. 2C, a
bubble column condenser 200 includes a vapor distribution chamber
244, a first stage 210, and a second stage 220. Vapor distribution
chamber 244, located at the bottom of condenser 200, includes a
liquid layer 234, which may be in direct contact with a liquid
outlet 242. Vapor distribution chamber 244 also includes a vapor
distribution region 236, which may be positioned above liquid layer
234 and may be in direct contact with a vapor inlet 240 in fluid
communication with a source of a vapor mixture (e.g., a gas or gas
mixture comprising a condensable liquid in a vapor phase). First
stage 210 includes a chamber 212, liquid layer 214 positioned
within chamber 212, bubble generator 208, and first liquid inlet
234 for the vapor mixture. First stage 210 also includes a first
vapor distribution region located above liquid layer 214 (e.g., the
portion of chamber 212 that is not occupied by liquid layer 214).
Second stage 220 includes a chamber 224, a liquid layer 226
positioned within chamber 224, a bubble generator 222, a liquid
inlet 232 for receiving a stream of the condensable fluid in liquid
phase (e.g., the liquid phase), and a vapor outlet 230. Second
stage 220 also includes a second vapor distribution region
positioned above liquid layer 226 (e.g., the portion of chamber 224
that is not occupied by liquid layer 226).
In operation, a vapor mixture may enter vapor distribution region
236 via vapor inlet 240. In vapor distribution region 236, the
vapor mixture may be substantially homogeneously distributed
throughout vapor distribution region 236. The vapor mixture may
then travel through bubble generator 208, and gas bubbles may form
and move through liquid layer 214, which may be maintained at a
temperature below that of the gas bubbles. As noted above, the gas
bubbles may undergo a condensation process and transfer heat and/or
mass of the condensable fluid to liquid layer 214. Bubbles of the
at least partially dehumidified vapor mixture may enter the first
vapor distribution region, and the at least partially dehumidified
vapor mixture may be substantially homogeneously distributed
throughout the first vapor distribution region. The at least
partially dehumidified vapor mixture may then enter bubble
generator 222 and form gas bubbles, which may travel through liquid
layer 226. Bubbles of the further dehumidified vapor mixture may
then enter the second vapor distribution region, and the further
dehumidified vapor mixture may be substantially homogeneously
distributed throughout the second vapor distribution region. The
vapor mixture may then exit bubble column condenser 200 through
vapor outlet 230 as a bubble column condenser gas outlet
stream.
Again referring to FIG. 2C, a stream of a condensable fluid in
liquid phase may enter second stage 220 via liquid inlet 232. The
liquid phase may first enter and be combined with liquid layer 226,
which may have a maximum height specified by weir 228. The liquid
phase may travel lengthwise across the surface of bubble generator
222, in the direction of arrow 246. If the height of liquid layer
226 exceeds the height of weir 228, excess liquid phase may flow
over the top of weir 228 through conduit/downcomer 218 to liquid
layer 214. The liquid phase may then flow across the surface of
bubble generator 208 in the direction of arrow 248. As shown in
FIG. 2C, the direction of arrow 248 may be opposite that of arrow
246. If the height of liquid layer 214 exceeds the height of weir
250, excess liquid phase may flow over the top of weir 250 through
conduit/downcomer 238 to liquid layer 234. The liquid phase may
then travel across the bottom surface of bottom chamber 244 in the
direction of arrow 252 and exit the bubble column condenser via
liquid outlet 242. As shown in FIG. 2C, the direction of arrow 252
may be opposite that of arrow 248.
Bubble condenser 200 may, in certain cases, further comprise
additional vapor inlets. For example, FIG. 2D shows an exemplary
illustration of a bubble column condenser 200 comprising a first
vapor distribution region 236, which includes a first vapor inlet
240, and a second vapor distribution region 212, which includes a
second vapor inlet 205. First vapor inlet 240 may be in fluid
communication with a source of a first vapor mixture. Second vapor
inlet 205 may be in fluid communication with a source of a second
vapor mixture.
In some cases, the first and second gases or gas mixtures may have
substantially the same composition. In some cases, the first and
second gases or gas mixtures may have different compositions. The
first and second gases or gas mixtures may, in certain cases, have
different vapor (e.g., water vapor) concentrations. In some
embodiments, the first and second gases or gas mixtures may have
substantially the same vapor concentration. In some cases, the
first and second gases or gas mixtures may be maintained at
different temperatures. The difference between the temperature of
the first and second gases or gas mixtures may, in certain
embodiments, be at least about 1.degree. C., at least about
5.degree. C., at least about 10.degree. C., at least about
20.degree. C., at least about 50.degree. C., at least about
100.degree. C., at least about 150.degree. C., or at least about
200.degree. C. In certain cases, the first and second gases or gas
mixtures may be maintained at substantially the same
temperature.
It should be understood that the bubble column condenser may have
any number of stages. In some embodiments, the bubble column
condenser may have at least one, at least two, at least three, at
least four, at least five, at least six, at least seven, at least
eight, at least nine, or at least ten or more stages. In some
embodiments, the bubble column condenser may have no more than one,
no more than two, no more than three, no more than four, no more
than five, no more than six, no more than seven, no more than
eight, no more than nine, no more than ten stages. The stages may
be vertically aligned, i.e., the stages may be arranged vertically
within the bubble column condenser, as shown in FIG. 2. In some
cases, the stages may be arranged such that the bottom surfaces of
the individual chambers (or bubble generators) are substantially
parallel to one another. In some cases, the stages may be arranged
such that the bottom surface of the individual chambers (or bubble
generators) are substantially non-parallel to one another. In some
embodiments, the stages may be positioned at an angle. The stages
may be horizontally aligned, i.e., the stages may be arranged
horizontally within the bubble column condenser. In some such
embodiments, at least one stage of the bubble condenser may
comprise a liquid layer, a vapor distribution region, a bubble
generator submerged in the liquid layer, and a gas outlet fluidly
connected to a bubble generator of another stage (e.g., an adjacent
stage).
In some cases, the condenser may be constructed as a modular system
such that various components or regions of the system are removable
and/or exchangeable. For example, the system may include an area
that can accommodate one or more stages, and can be readily
configured to include a desired number of stages. FIG. 7B shows an
illustrative embodiment where the system includes eight trays,
allowing for a capacity for one to eight stages. Each stage can be
added or removed by simply sliding the stage in and out of the
system. In embodiments such as this, the number and distance
between stages may be readily tailored to suit a particular
application.
The stages of the condenser may have any shape suitable for a
particular application. In some embodiments, at least one stage of
the condenser has a cross sectional shape that is substantially
circular, substantially elliptical, substantially square,
substantially rectangular, and/or substantially triangular. In
certain embodiments, each stage of the condenser has a cross
sectional shape that is substantially circular, substantially
elliptical, substantially square, substantially rectangular, and/or
substantially triangular. In some cases, the stages of the
condenser have a relatively large aspect ratio. As used herein, the
aspect ratio of an individual stage refers to the ratio of the
length of the individual stage to the width of the individual
stage. The length of an individual stage refers to the largest
internal cross-sectional dimension of the stage (e.g., in a plane
perpendicular to a vertical axis of the stage). For example, in
FIG. 1A, the length of stage 110 is indicated as L.sub.S. To
further illustrate length, FIG. 1B provides an exemplary top-down
view of stage 110 (e.g., looking down on bubble generator 160).
That is, FIG. 1B is an exemplary schematic illustration of a plane
perpendicular to a vertical axis of stage 110 (e.g., a
cross-sectional plane). In FIG. 1B, the length of stage 110 is
indicated as L.sub.S. The width of an individual stage generally
refers to the largest cross-sectional dimension of the stage (e.g.,
in a plane perpendicular to a vertical axis of the stage) measured
perpendicular to the length. In FIG. 1B, the width of stage 110 is
indicated as W.sub.S.
In some embodiments, at least one stage has an aspect ratio of at
least about 1.5, at least about 2, at least about 5, at least about
10, at least about 15, or at least about 20. In some embodiments,
at least one stage has an aspect ratio in the range of about 1.5 to
about 5, about 1.5 to about 10, about 1.5 to about 15, about 1.5 to
about 20, about 2 to about 5, about 2 to about 10, about 2 to about
15, about 2 to about 20, about 5 to about 10, about 5 to about 15,
about 5 to about 20, about 10 to about 15, about 10 to about 20, or
about 15 to about 20. In some embodiments, each stage of the
condenser has an aspect ratio of at least about 1.5, at least about
2, at least about 5, at least about 10, at least about 15, or at
least about 20. In some embodiments, each stage of the condenser
has an aspect ratio in the range of about 1.5 to about 5, about 1.5
to about 10, about 1.5 to about 15, about 1.5 to about 20, about 2
to about 5, about 2 to about 10, about 2 to about 15, about 2 to
about 20, about 5 to about 10, about 5 to about 15, about 5 to
about 20, about 10 to about 15, about 10 to about 20, or about 15
to about 20.
In some embodiments, the height of the liquid layer within at least
one stage of the bubble column condenser is relatively low during
substantially continuous operation. Generally, a water desalination
system is said to be operated substantially continuously when an
aqueous stream is being fed to the desalination system at the same
time that a desalinated product stream is being produced by the
desalination system. The height of the liquid layer within a stage
can be measured from the surface of the bubble generator that
contacts the liquid layer to the top surface of the liquid layer.
As noted herein, having a relatively low level of liquid phase in
at least one stage may, in some embodiments, advantageously result
in a low pressure drop between the inlet and outlet of an
individual stage. Without wishing to be bound by a particular
theory, the pressure drop across a given stage of the condenser may
be due, at least in part, to the hydrostatic head of the liquid in
the stage that the gas has to overcome. Therefore, the height of
the liquid layer in a stage may be advantageously kept low to
reduce the pressure drop across that stage.
In some embodiments, during substantially continuous operation of
the bubble column condenser, the liquid layer within at least one
stage of the condenser has a height of (e.g., the height of
condensable fluid within a stage is) less than about 0.1 m, less
than about 0.09 m, less than about 0.08 m, less than about 0.07 m,
less than about 0.06 m, less than about 0.05 m, less than about
0.04 m, less than about 0.03 m, less than about 0.02 m, less than
about 0.01 m, or, in some cases, less than about 0.005 m. In some
embodiments, during substantially continuous operation of the
bubble column condenser, the liquid layer within each stage of the
condenser has a height of less than about 0.1 m, less than about
0.09 m, less than about 0.08 m, less than about 0.07 m, less than
about 0.06 m, less than about 0.05 m, less than about 0.04 m, less
than about 0.03 m, less than about 0.02 m, less than about 0.01 m,
or, in some cases, less than about 0.005 m.
In condensers described herein, the ratio of the height of the
liquid layer (e.g., water) in a stage of the condenser to the
length of the stage of the condenser may be relatively low. The
length of the stage of the condenser generally refers to the
largest internal cross-sectional dimension of the stage of the
condenser. In some embodiments, the ratio of the height of the
liquid layer within at least one stage of the bubble column
condenser during steady-state operation to the length of the at
least one stage of the condenser is less than about 1, less than
about 0.8, less than about 0.6, less than about 0.4, less than
about 0.2, less than about 0.18, less than about 0.16, less than
about 0.14, less than about 0.12, less than about 0.1, or, in some
cases, less than about 0.05. In some embodiments, the ratio of the
height of the liquid layer within each stage of the bubble column
condenser during steady-state operation to the length of each
corresponding stage of the condenser is less than about 1, less
than about 0.8, less than about 0.6, less than about 0.4, less than
about 0.2, less than about 0.18, less than about 0.16, less than
about 0.14, less than about 0.12, less than about 0.1, or, in some
cases, less than about 0.05.
In some embodiments, the height of an individual stage within the
condenser (e.g., measured vertically from the bubble generator
positioned at the bottom of the stage to the top of the chamber
within the stage) may be relatively small. As noted above, reducing
the height of one or more stages of the condenser may potentially
reduce costs and/or potentially increase heat and mass transfer
within the system. In some embodiments, the height of at least one
stage is less than about 0.5 m, less than about 0.4 m, less than
about 0.3 m, less than about 0.2 m, less than about 0.1 m, or, in
some cases, less than about 0.05 m. In some embodiments, the height
of each stage is less than about 0.5 m, less than about 0.4 m, less
than about 0.3 m, less than about 0.2 m, less than about 0.1 m, or,
in some cases, less than about 0.05 m. The total height of the
condenser column may, in some embodiments, be less than about 10 m,
less than about 8 m, less than about 6 m, less than about 4 m, less
than about 2 m, less than about 1 m, or, in some cases, less than
about 0.5 m.
In some embodiments, the pressure drop across a stage (i.e. the
difference between inlet gas pressure and outlet gas pressure) for
at least one stage in the bubble column condenser is less than
about 2000 Pa, less than about 1500 Pa, less than about 1000 Pa,
less than about 800 Pa, less than about 500 Pa, less than about 200
Pa, less than about 100 Pa, or, in some cases, less than about 50
Pa. In some embodiments, the difference between bubble column
condenser inlet gas pressure and bubble column condenser outlet gas
pressure is less than about 2000 Pa, less than about 1500 Pa, less
than about 1000 Pa, less than about 800 Pa, less than about 500 Pa,
less than about 200 Pa, less than about 100 Pa, or, in some cases,
less than about 50 Pa.
In some embodiments, the bubble column condenser may exhibit
improved heat transfer properties. For example, when the bubble
column condenser is in substantially continuous operation, the heat
transfer coefficient may be at least about 2000 W/(m.sup.2 K), at
least about 3000 W/(m.sup.2 K), at least about 4000 W/(m.sup.2 K),
or, in some cases, at least about 5000 W/(m.sup.2 K).
In some cases, the temperature of the condenser liquid inlet stream
may be different than the temperature of the condenser liquid
outlet stream. For example, during substantially continuous
operation of the bubble column condenser, the temperature of the
condenser liquid inlet stream may be less than about 100.degree.
C., less than about 90.degree. C., less than about 80.degree. C.,
less than about 70.degree. C., less than about 60.degree. C., less
than about 50.degree. C., less than about 45.degree. C., less than
about 40.degree. C., less than about 30.degree. C., less than about
20.degree. C., or, in some cases, less than about 10.degree. C. In
some cases, the temperature of the condenser liquid inlet stream
may range from about 0.degree. C. to about 100.degree. C., from
about 10.degree. C. to about 90.degree. C., or from about
20.degree. C. to about 80.degree. C. During substantially
continuous operation of the bubble column condenser, the
temperature of the condenser liquid outlet stream may be at least
about 50.degree. C., at least about 60.degree. C., at least about
70.degree. C., at least about 80.degree. C., at least about
85.degree. C., at least about 90.degree. C., or at least about
100.degree. C. In some cases, the temperature of the condenser
liquid outlet stream may range from about 50.degree. C. to about
100.degree. C., from about 60.degree. C. to about 90.degree. C., or
from about 60.degree. C. to about 85.degree. C. The difference in
inlet and outlet liquid temperature may be at least about 5.degree.
C., at least about 10.degree. C., at least about 20.degree. C., or,
in some cases, at least about 30.degree. C. In some cases, the
difference in inlet and outlet temperature may range from about
5.degree. C. to about 30.degree. C., from about 10.degree. C. to
about 30.degree. C., or from about 20.degree. C. to about
30.degree. C.
In some embodiments, the gas or gas mixture may travel through the
condenser at a relatively high flow rate. It may be advantageous,
in certain embodiments, for gas flow rate to be relatively high
since heat and mass transfer coefficients are generally higher at
higher gas flow rates. In some embodiments, the gas or gas mixture
may have a flow rate of at least about 10 cubic foot per minute
(cfm) per square foot (ft.sup.2), at least about 20 cfm/ft.sup.2,
at least about 40 cfm/ft.sup.2, at least about 60 cfm/ft.sup.2, at
least about 80 cfm/ft.sup.2, at least about 100 cfm/ft.sup.2, at
least about 120 cfm/ft.sup.2, at least about 140 cfm/ft.sup.2, at
least about 160 cfm/ft.sup.2, at least about 180 cfm/ft.sup.2, or,
in some cases, at least about 200 cfm/ft.sup.2. In some
embodiments, the gas or gas mixture may have a flow rate in the
range of about 10 cfm/ft.sup.2 to about 200 cfm/ft.sup.2, about 20
cfm/ft.sup.2 to about 200 cfm/ft.sup.2, about 40 cfm/ft.sup.2 to
about 200 cfm/ft.sup.2, about 60 cfm/ft.sup.2 to about 200
cfm/ft.sup.2, about 80 cfm/ft.sup.2 to about 200 cfm/ft.sup.2,
about 100 cfm/ft.sup.2 to about 200 cfm/ft.sup.2, about 120
cfm/ft.sup.2 to about 200 cfm/ft.sup.2, about 140 cfm/ft.sup.2 to
about 200 cfm/ft.sup.2, about 160 cfm/ft.sup.2 to about 200
cfm/ft.sup.2, or about 180 cfm/ft.sup.2 to about 200
cfm/ft.sup.2.
In some embodiments, the gas or gas mixture may contain a certain
amount of water (e.g., may be "humidified") such that, after
flowing through the condenser, the gas or gas mixture may be
substantially dehumidified relative to the gas or gas mixture prior
to flowing through the condenser. At a given set of system
conditions, the gas or gas mixture may have a relative humidity.
Relative humidity generally refers to the ratio of the partial
pressure of water vapor in a mixture of air and water to the
saturated vapor pressure of water at a given temperature. In some
embodiments, the relative humidity of the gas or gas mixture at at
least one gas inlet to the bubble column condenser may be at least
about 70%, at least about 80%, at least about 90%, or about 100%.
In some embodiments, the relative humidity of the gas at a gas
outlet to the bubble column condenser may be less than about 20%,
less than about 10%, less than about 5%, or about 0%.
In some embodiments, the bubble column condenser comprises at least
one bubble generator. Examples of types of bubble generators
include sieve plates, spargers, and nozzle-type bubble generators.
In some embodiments, a bubble generator may comprise a plurality of
perforations through which vapor can travel. The bubble generators
may be operated at various bubble generator speeds, with various
features (e.g., holes) used for generation of bubbles, or the like.
The selection of bubble generator can affect the size and/or shape
of the gas bubbles, thereby affecting heat transfer from the gas
bubbles to the condensable fluid in a liquid phase. Those of
ordinary skill in the art are capable of selecting the appropriate
bubble generator and/or bubble generator conditions in order to
produce a particular desired set of gas bubbles. In some
embodiments, the bubble generator comprises a sparger plate. It has
been recognized that a sparger plate may have certain advantageous
characteristics. For example, the pressure drop across a sparger
plate may be low. Additionally, the simplicity of the sparger plate
may render it inexpensive to manufacture and/or resistant to the
effects of fouling. The sparger plate may, in some embodiments,
comprise a plurality of holes. In some embodiments, at least a
portion of the plurality of holes have a diameter (or smallest
cross-sectional dimension of a line passing through the geometric
center of the hole for non-circular holes) in the range of about
0.1 mm to about 50 mm, about 0.1 mm to about 25 mm, about 0.1 mm to
about 15 mm, or, in some cases, about 1 mm to about 15 mm. In some
embodiments, at least a portion of the plurality of holes have a
diameter of about 1 mm, about 2 mm, about 3 mm, about 3.2 mm, or,
in some cases, about 4 mm. In some cases, the sparger plate may be
arranged along the bottom surface of an individual stage within the
condenser. In some cases, the surface area of the sparger plate may
be selected such that it covers at least approximately 50%, at
least approximately 60%, at least approximately 70%, at least
approximately 80%, at least approximately 90%, or approximately
100% of a cross-section of the condenser. In some embodiments, the
bubble generator comprises one or more perforated pipes. The
perforated pipes, which can extend from a central conduit, can
feature, for example, a radial, annular, spider-web, or
hub-and-spoke configuration through which the gas or gas mixture is
pumped from an external source. In some embodiments, at least one
bubble generator may be coupled to the inlet of a stage. In some
embodiments, a bubble generator is coupled to the inlet of each
stage of the bubble column condenser.
The condensers described herein may further include one or more
components positioned to facilitate, direct, or otherwise affect
flow of a fluid within the condenser. In some embodiments, at least
one chamber of at least one stage of the bubble column condenser
may include one or more baffles positioned to direct flow of a
fluid, such as a stream of the condensable fluid in liquid phase
(e.g., water). In certain cases, each chamber of the bubble column
condenser may comprise one or more baffles. Suitable baffles for
use in embodiments described herein include plate-like articles
having, for example, substantially rectangular-shape, as shown by
the illustrative embodiments in FIG. 6. Baffles may also be
referred to as barriers, dams, or the like.
The baffle, or combination of baffles, may be arranged in various
configurations so as to direct the flow of a liquid within the
chamber. In some cases, the baffle(s) can be arranged such that
liquid travels in a substantially linear path from one end of the
chamber to the other end of the chamber (e.g., along the length of
a chamber having a substantially rectangular cross-section). In
some cases, the baffle(s) can be arranged such that liquid travels
in a non-linear path across a chamber, such a path having one or
more bends or turns within the chamber. That is, the liquid may
travel a distance within the chamber that is longer than the length
of the chamber. In some embodiments, one or more baffles may be
positioned along a bottom surface of at least one chamber within a
bubble column condenser, thereby affecting the flow of liquid that
enters the chamber.
In some embodiments, a baffle may be positioned in a manner so as
to direct flow of a liquid within a single chamber, e.g., along a
bottom surface of a chamber in either a linear or non-linear
manner. In some embodiments, one or more baffles may be positioned
substantially parallel to the transverse sides (i.e., width) of a
chamber having a substantially rectangular cross-sectional shape,
i.e., may be a transverse baffle. In some embodiments, one or more
baffles may be positioned substantially parallel to the
longitudinal sides (i.e., length) of a chamber having a
substantially rectangular cross-sectional shape, i.e., may be a
longitudinal baffle. In such configurations, one or more
longitudinal baffles may direct the flow of liquid along a
substantially non-linear path.
In some embodiments, one or more baffles may be positioned in a
manner so as to direct flow of a liquid within a single chamber
along a path that may promote efficiency of heat and/or mass
transfer. For example, a chamber may comprise a liquid entering
through a liquid inlet at a first temperature and a gas or gas
mixture entering through a bubble generator at a second, different
temperature. In certain cases, heat and mass transfer between the
liquid and the gas or gas mixture may be increased when the first
temperature approaches the second temperature. One factor that may
affect the ability of the first temperature to approach the second
temperature may be the amount of time the liquid spends flowing
through the chamber.
In some cases, it may be advantageous for portions of the liquid
flowing through the chamber to spend substantially equal amounts of
time flowing through the chamber. For example, heat and mass
transfer may undesirably be reduced under conditions where a first
portion of the liquid spends a shorter amount of time in the
chamber and a second portion of the liquid spends a longer amount
of time in the chamber. Under such conditions, the temperature of a
mixture of the first portion and the second portion may be further
from the second temperature of the gas or gas mixture than if both
the first portion and the second portion had spent a substantially
equal amount of time in the chamber. Accordingly, in some
embodiments, one or more baffles may be positioned in the chamber
to facilitate liquid flow such that portions of the liquid flowing
through the chamber spend substantially equal amounts of time
flowing through the chamber. For example, one or more baffles
within the chamber may spatially separate liquid located at the
inlet (e.g., liquid likely to have spent a shorter amount of time
in the chamber) from liquid located at the outlet (e.g., liquid
likely to have spent a longer amount of time in the chamber). In
some cases, one or more baffles within the chamber may facilitate
liquid flow along flow paths having substantially the same length.
For example, the one or more baffles may prevent a first portion of
liquid from travelling along a substantially shorter path from the
inlet of the chamber to the outlet of the chamber (e.g., along the
width of a chamber having a rectangular cross section) and a second
portion of liquid from travelling along a substantially longer path
from the inlet of the chamber to the outlet of the chamber (e.g.,
along the length of a chamber having a rectangular cross
section).
In some cases, it may be advantageous to increase the amount of
time a liquid spends flowing through a chamber. Accordingly, in
certain embodiments, one or more baffles may be positioned within a
single chamber to facilitate liquid flow along a flow path having a
relatively high aspect ratio (e.g., the ratio of the average length
of the flow path to the average width of the flow path). For
example, in some cases, one or more baffles may be positioned such
that liquid flowing through the chamber follows a flow path having
an aspect ratio of at least about 1.5, at least about 2, at least
about 5, at least about 10, at least about 20, at least about 50,
at least about 75, or at least about 100.
In some cases, the aspect ratio of a liquid flow path through a
chamber may be larger than the aspect ratio of the chamber. In
certain cases, the presence of baffles to increase the aspect ratio
of a liquid flow path may facilitate the use of an apparatus having
a relatively low aspect ratio (e.g., about 1), such as an apparatus
having a substantially circular cross section. For example, FIG. 12
shows an exemplary schematic illustration of a chamber 1200 having
a substantially circular cross section (e.g., bottom surface) and a
spiral baffle 1202. In operation, liquid may enter chamber 1200
through a liquid inlet (not shown) positioned at or near the center
of the substantially circular cross section. The liquid may then
flow along spiral baffle 1202 and exit chamber 1200 through a
liquid outlet (not shown) positioned at the upper edge of the
substantially circular cross section. While the substantially
circular cross section of chamber 1200 has an aspect ratio of about
1, the aspect ratio of the liquid flow path is substantially
greater than 1 (e.g., approximately 4.5). As an additional example,
FIG. 13 shows an exemplary schematic illustration of a chamber 1300
having a substantially circular cross section (e.g., bottom
surface) and comprising a first baffle 1302 and a second baffle
1304. In operation, liquid may enter chamber 1300 through a liquid
inlet (not shown) located in the upper left portion of the
substantially circular cross section. The liquid may first flow in
the direction of arrow 1306. The liquid may then flow around baffle
1302 and flow in the opposite direction, in the direction of arrow
1308. The liquid may then flow around baffle 1304 and flow in the
direction of arrow 1310 and subsequently exit chamber 1300 through
a liquid outlet (not shown) located in the lower right portion of
the substantially circular cross section. While the aspect ratio of
the circular cross section of chamber 1300 is about 1, the aspect
ratio of the liquid flow path through chamber 1300 is substantially
greater than 1.
In some embodiments, one or more weirs may be positioned within the
chamber in a manner so as to control or direct flow of a liquid
between two chambers. For example, a weir may be positioned
adjacent or surrounding a region of the chamber that receives a
stream of liquid, for example, from a different chamber above the
region. In some cases, a weir may be positioned adjacent or
surrounding a region of the chamber where liquid may flow out of
the chamber, for example, into a different chamber below. In some
cases, a weir may be positioned within a chamber so as to not
contact one or more walls of the chamber. In some cases, a weir may
be positioned within a chamber so as to contact one or more walls
of the chamber.
The one or more weirs may be selected to have a height that is less
than the height of the chamber. In some embodiments, the height of
the weirs may determine the maximum height for a liquid phase or
layer in the chamber. For example, if a liquid layer residing in a
first chamber reaches a height that exceeds the height of a weir
positioned along a bottom surface of the chamber, then at least a
portion of the excess liquid layer may flow over the weir. In some
cases, the excess liquid may flow into a second, adjacent chamber,
e.g., a chamber positioned below the first chamber. In some
embodiments, at least one weir in a chamber may have a height of
less than about 0.1 m, less than about 0.09 m, less than about 0.08
m, less than about 0.07 m, less than about 0.06 m, less than about
0.05 m, less than about 0.04 m, less than about 0.03 m, less than
about 0.02 m, less than about 0.01 m, or, in some cases, less than
about 0.005 m. In some embodiments, each weir in a chamber may have
a height of less than about 0.1 m, less than about 0.09 m, less
than about 0.08 m, less than about 0.07 m, less than about 0.06 m,
less than about 0.05 m, less than about 0.04 m, less than about
0.03 m, less than about 0.02 m, less than about 0.01 m, or, in some
cases, less than about 0.005 m.
In some embodiments, one or more weirs may be positioned to promote
the flow of a liquid across the length of the chamber in a
substantially linear path. For example, the chamber may be selected
to have a cross-sectional shape having a length that is greater
than its width (e.g., a substantially rectangular cross-section),
such that the weirs promote flow of liquid along the length of the
chamber. In some cases, it may be desirable to promote such cross
flow across a chamber to maximize the interaction, and therefore
heat and/or mass transfer, between the liquid phase and the vapor
phase of a condensable fluid.
In one embodiment, a chamber may include a first weir and a second
weir positioned along the bottom surface of the chamber. The first
and second weirs may be positioned at opposite ends of the chamber
lengthwise, such that a stream of condensable fluid in liquid phase
may flow along the length of the chamber from the first weir to the
second weir. One example of a bubble generator system having such a
configuration is illustrated in FIG. 7H. In FIG. 7H, bubble
generator 702 (which can include a plurality of perforations)
includes a first weir 704 positioned at one end of the bubble
generator. Bubble generator 702 further comprises second weir 706
and third weir 708, both of which are positioned at the opposite
end of the bubble generator as first baffle 704. In operation, a
liquid may be introduced to the bubble generator and may flow to
region 704a surrounded by weir 704. As additional liquid is
introduced and the height of the liquid in region 704a exceeds the
height of weir 704, excess liquid may flow over the top of weir 704
and flow across the surface of bubble generator 702 in the
direction of arrow 710 across bubble generator 702. If the height
of the liquid then exceeds the height of weir 706 and/or 708,
excess liquid may flow over the top of weir 706 and/or weir 708 and
flow to another portion of the apparatus. In some cases, excess
liquid may flow to a chamber positioned below bubble generator
702.
In some embodiments, a bubble column condenser may include a
plurality of chambers arranged in a vertical stack, and one or more
weirs and/or baffles may be positioned in one or more chambers such
that a liquid can flow across the length of the chamber. In some
cases, the chambers can be arranged such that liquid flows in
opposing directions for adjacent chambers. For example, a bubble
column condenser may comprise a first chamber and a second chamber,
and one or more weirs and/or baffles may be positioned in each of
the first and second chambers such that a stream of condensable
fluid in liquid phase flows along the length of the first chamber
in a first direction and along the length of the second chamber in
a second, opposing direction. For example, FIG. 2C illustrates a
configuration in which a bubble column condenser 200 comprises a
vapor distribution chamber 244, a first stage 210 comprising a
chamber 212, and a second stage 220 comprising a chamber 224. A
stream of a condensable fluid in liquid phase may enter condenser
200 through liquid inlet 232, and the liquid stream may flow across
second stage 220 in the direction of arrow 246. In first stage 210
positioned vertically below second stage 220, excess liquid stream
from second stage 200 may enter first stage 10 and may flow across
first stage 210 in the direction of arrow 248, where the direction
of arrow 248 is opposite that of arrow 246. In vapor distribution
chamber 244 positioned vertically below first stage 210, excess
liquid stream from first stage 210 may flow in the direction of
arrow 252, where the direction of arrow 252 is in substantially the
opposite direction as arrow 248 and substantially the same
direction as arrow 246.
In some embodiments, a first weir may be positioned adjacent an
area that receives a liquid stream (e.g., from a liquid inlet, or
from a region above the first weir). The first weir may be
positioned at the opposite end, lengthwise, from a second weir
positioned adjacent an outlet or a down corner that may deliver
excess liquid to another region of the apparatus. In some
embodiments, the first weir and the second weir may be positioned
at the same end of the first chamber.
Some embodiments involve the use of both weirs and baffles to
direct liquid flow within and between chambers. In some cases, the
baffle may be a longitudinal baffle. In some cases, the baffle may
be a transverse baffle (e.g., a horizontal baffle). One such
embodiment is illustrated in FIG. 6, where a longitudinal baffle
604, weir 606, and weir 608 are positioned on a bubble generator
602. Weir 606 and weir 608 are positioned at a first end of bubble
generator 602. Longitudinal baffle 604 extends along the length of
bubble generator 602, from the first end of bubble generator 602
toward the second, opposing end of bubble generator 602. The length
of longitudinal baffle 604 is less than the length of the bubble
generator, providing a gap between the end of longitudinal baffle
604 and the second, opposing end of bubble generator 602 for a
liquid to flow.
When system 600 is in use, weir 606 may receive a stream of a
condensable fluid in liquid phase. The liquid may reside within
region 606a enclosed by weir 606. As additional liquid is
introduced and the height of the liquid in enclosed region 606a
exceeds the height of weir 606, excess liquid may flow over the top
of weir 606 and flow along the length of bubble generator 602, in
the direction of arrow 610 as directed by longitudinal baffle 604.
The liquid phase may then flow across the width of the bubble
generator 602 via the gap between longitudinal baffle 604 and a
transverse wall of the chamber. Liquid may then flow along the
length of bubble generator 602 in the direction of arrow 612, which
is opposite that of arrow 610. When the height of the liquid
exceeds the height of weir 608, excess liquid may flow over the top
of weir 608 and into another portion of the apparatus. It should be
understood that a chamber may include comprise more than one
longitudinal baffle. In some embodiments, at least one longitudinal
baffle, at least two longitudinal baffles, at least three
longitudinal baffles, at least four longitudinal baffles, at least
five longitudinal baffles, at least ten longitudinal baffles, or
more, are arranged within the chamber. In some embodiments, the
chamber includes 1-10 longitudinal baffles, 1-5 longitudinal
baffles, or, 1-3 longitudinal baffles.
In some cases, at least one transverse baffle, at least two
transverse baffles, at least three transverse baffles, at least
four transverse baffles, at least five transverse baffles, at least
ten transverse baffles, or more, are arranged within the chamber.
In some embodiments, the chamber includes 1-10 transverse baffles,
1-5 transverse baffles, or, 1-3 transverse baffles.
The bubble column condenser may have any shape suitable for a
particular application. In some embodiments, the bubble column
condenser may have a cross section that is substantially circular,
substantially elliptical, substantially square, substantially
rectangular, or substantially triangular. It has been recognized
that it may be advantageous for a bubble column condenser to have a
substantially circular cross section. In some cases, a bubble
column condenser having a substantially circular cross section
(e.g., a substantially cylindrical bubble column condenser) may be
easier to manufacture than a bubble column condenser having a cross
section of a different shape (e.g., a substantially rectangular
cross section). For example, for a substantially cylindrical bubble
column condenser having a certain diameter (e.g., about 0.6 m or
less), prefabricated pipes and/or tubes may be used to form the
walls of the bubble column. In addition, a substantially
cylindrical bubble column condenser may be manufactured from a
sheet material (e.g., stainless steel) by bending the sheet and
welding a single seam. In contrast, a bubble column condenser
having a cross section of a different shape may have more than one
welded seam (e.g., a bubble column condenser having a substantially
rectangular cross section may have four welded seams). Further, a
bubble column condenser having a substantially circular cross
section may require less material to fabricate than a bubble column
condenser having a cross section of a different shape (e.g., a
substantially rectangular cross section). In certain embodiments,
the bubble column condenser has a substantially parallelepiped
shape, a substantially rectangular prism shape, a substantially
cylindrical shape, and/or a substantially pyramidal shape.
The bubble column condenser may have any size suitable for a
particular application. In some embodiments, the largest
cross-sectional dimension of the bubble column condenser may be
less than about 10 m, less than about 5 m, less than about 2 m,
less than about 1 m, less than about 0.5 m, or less than about 0.1
m. In some cases, the largest cross-sectional dimension of the
bubble column condenser may range from about 10 m to about 0.01 m,
from about 5 m to about 0.5 m, or from about 5 m to about 1 m.
The exterior of the bubble column condenser may comprise any
suitable material. In certain embodiments, the bubble column
condenser comprises stainless steel, aluminum, and/or a plastic
(e.g., polyvinyl chloride, polyethylene, polycarbonate). In some
embodiments, it may be advantageous to minimize heat loss from the
bubble column condenser to the environment. In some cases, the
exterior of the condenser and/or the interior of the condenser may
comprise a thermally insulating material. For example, the
condenser may be at least partially coated, covered, or wrapped
with a thermally insulating material. Non-limiting examples of
suitable thermally insulating materials include elastomeric foam,
fiberglass, ceramic fiber mineral wool, glass mineral wool,
phenolic foam, polyisocyanurate, polystyrene and polyurethane.
While the features described above have been discussed in the
context of condensing apparatuses such as bubble column condensers,
all of the described features (e.g., shape, aspect ratio, presence
of weirs and/or baffles, etc.) may also be applied to humidifying
apparatuses, such as bubble column humidifiers. Use of a bubble
column humidifier may, in some cases, be advantageous compared to
use of other types of humidifiers (e.g., packed bed humidifiers)
for many of the same reasons that use of a bubble column condenser
may be advantageous compared to other types of condensers. For
example, a bubble column humidifier may be characterized by
improved performance (e.g., higher rates of heat and/or mass
transfer, higher thermodynamic effectiveness) and/or reduced
fabrication and/or material costs (e.g., reduced dimensions)
compared to other types of humidifiers.
In certain cases, a bubble column humidifier comprises a plurality
of stages (e.g., the bubble column humidifier is a multi-stage
bubble column humidifier). The stages may be arranged such that a
gas stream (e.g., an air stream) flows sequentially through a first
stage, a second stage, a third stage, and so on. In some
embodiments, each stage comprises a liquid layer having a
temperature, and the temperature of the liquid layer of a stage may
be lower than the temperature of subsequent stages. For example, in
a three-stage bubble column humidifier, the temperature of the
liquid layer of the first stage (e.g., the bottommost stage in a
vertically arranged bubble column) may be lower than the
temperature of the liquid layer of the second stage, which may be
lower than the temperature of the liquid layer of the third stage
(e.g., the topmost stage in a vertically arranged bubble column).
Within each stage, heat and mass may be transferred from the liquid
layer to bubbles of the gas stream.
To illustrate the operation of a multi-stage bubble column
humidifier, the operation of an exemplary embodiment of a
multi-stage bubble column humidifier, as illustrated in FIG. 2A, is
described. According to some embodiments, apparatus 200 of FIG. 2A
is a multi-stage bubble column humidifier. Bubble column humidifier
200 comprises all of the components previously discussed in the
context of a bubble column condenser (e.g., first stage 210
comprising liquid layer 214 and bubble generator 208, second stage
220 comprising liquid layer 226 and bubble generator 222). However,
liquid layers 214 and 226 comprise salt-containing water instead of
substantially pure condensable fluid in a liquid phase.
Additionally, the temperature of the salt-containing water of
liquid layers 214 and 226 is higher than the temperature of a first
gas or gas mixture flowing through bubble column humidifier
200.
In operation, a gas or gas mixture may travel through bubble
generator 208, thereby forming bubbles. As the gas or gas mixture
bubbles subsequently travel through liquid layer 214, which is
maintained at a temperature above that of the gas or gas mixture,
heat and mass are transferred from the salt-containing water of
liquid layer 214 to the bubbles of the gas or gas mixture, thereby
at least partially humidifying the gas or gas mixture. The at least
partially humidified gas or gas mixture may then travel through a
first vapor distribution region and enter bubble generator 222,
forming bubbles of the at least partially humidified gas or gas
mixture. Bubbles of the at least partially humidified gas or gas
mixture may then travel through liquid layer 226, which has a
temperature higher than the temperature of liquid layer 214, and
heat and mass may be transferred from liquid layer 226 to the
bubbles of the at least partially humidified gas or gas mixture,
further humidifying the gas or gas mixture.
The bubble column humidifier may comprise any suitable material
(e.g., a material that is heat-resistant and corrosion-resistant).
Non-limiting examples of suitable materials include chlorinated
polyvinyl chloride, polyethylene, fiberglass-reinforced plastic,
titanium alloys, Hastelloys (e.g., corrosion-resistant nickel
alloys), superalloys (e.g., molybdenum-based superalloys), and/or
epoxy-coated metals.
Some embodiments relate to systems comprising a bubble column
condenser as described herein arranged to be in fluid communication
with an external heat exchanger. In such embodiments, heat may be
transferred from a condenser liquid outlet stream to a coolant
stream flowing through the external heat exchanger. The system can
be configured such that the cooled condenser liquid outlet stream
can then be returned to the bubble column condenser through an
inlet and be re-used as a liquid to form liquid layers in the
stage(s) of the condenser. In this manner, the temperature of the
liquid layers within the bubble column condenser can be regulated
such that, in each stage, the temperature of the liquid layer is
maintained at a temperature lower than the temperature of the gas
or gas mixture. In some cases, arrangement of the heat exchanger at
a location that is external to the condenser, rather than at a
location that is within the condenser, can allow for use of
condensers as described herein (e.g., condensers having reduced
dimensions and/or reduced levels of liquid baths, etc.). In some
cases, the heat exchanger may transfer heat absorbed from the
condenser liquid outlet stream to another fluid.
FIG. 3A shows an exemplary embodiment of a system 300 including a
bubble column condenser 302 fluidly connected to an external heat
exchanger 304 via conduits 306 and 308. Heat exchanger 304 further
includes a coolant during operation. In operation, a condenser
liquid outlet stream containing an amount of absorbed heat exits
condenser 302 via conduit 306 at a temperature T.sub.1 and enters
external heat exchanger 304. Heat is transferred from the condenser
liquid outlet stream to the coolant, which is maintained at a
temperature T.sub.3 that is lower than temperature T.sub.1 of the
condenser liquid outlet stream. The condenser liquid outlet stream
then exits heat exchanger 304 via conduit 308 at temperature
T.sub.2, where T.sub.2 is less than T.sub.1, and is returned to
condenser 302 via conduit 308.
Heat exchanger 304 may optionally transfer any absorbed heat from
the condenser liquid outlet stream to another fluid stream. For
example, a heat exchanger inlet stream (e.g., a heat exchanger
coolant stream) may enter heat exchanger 304 via conduit 310 at
temperature T.sub.3. As the heat exchanger inlet stream passes
through heat exchanger 304, it may absorb heat transferred from the
condenser liquid outlet stream. The heat exchanger inlet stream may
then exit heat exchanger 304 via conduit 312 as a heat exchanger
outlet stream at temperature T.sub.4, where T.sub.4 is greater than
T.sub.3. In some embodiments, the condenser liquid inlet stream
flowing through conduit 308 and heat exchanger inlet stream flowing
through conduit 310 may be substantially the same. In other
embodiments, the condenser liquid inlet stream and the heat
exchanger inlet stream may be different. In some cases, the
condenser liquid outlet stream flowing through heat exchanger 304
(e.g., the stream flowing through conduits 306 and 308) and the
heat exchanger coolant stream (e.g., the stream flowing through
conduits 310 and 312) may flow in substantially parallel directions
through heat exchanger 304. In other embodiments (as illustrated),
the condenser liquid outlet stream flowing through heat exchanger
304 and the heat exchanger coolant stream may flow in substantially
non-parallel (e.g., opposite) directions through heat exchanger
304.
Any heat exchanger known in the art may be used. Examples of
suitable heat exchangers include, but are not limited to, plate and
frame heat exchangers, shell and tube heat exchangers, tube and
tube heat exchangers, plate heat exchangers, plate and shell heat
exchangers, and the like. In a particular embodiment, the heat
exchanger is a plate and frame heat exchanger. The heat exchanger
may be configured such that a first fluid stream and a second fluid
stream flow through the heat exchanger. In some cases, the first
fluid stream and the second fluid stream may flow in substantially
the same direction (e.g., parallel flow), substantially opposite
directions (e.g., counter flow), or substantially perpendicular
directions (e.g., cross flow). The first fluid stream may comprise,
in certain cases, a fluid stream that flows through a condenser
(e.g., a condenser liquid outlet stream). In some embodiments, the
second fluid stream may comprise a coolant. The first fluid stream
and/or the second fluid stream may comprise a liquid. In some
embodiments, the heat exchanger may be a liquid-to-liquid heat
exchanger. In some cases, more than two fluid streams may flow
through the heat exchanger.
The coolant may be any fluid capable of absorbing and transferring
heat. Typically, the coolant is a liquid. The coolant may, in some
embodiments, include water. In certain cases, the coolant may
include salt-containing water. For example, in a
humidification-dehumidification system, the coolant stream in the
heat exchanger may be used to preheat salt-containing water prior
to entry into a humidifier.
In some embodiments, the heat exchanger may exhibit relatively high
heat transfer rates. In some embodiments, the heat exchanger may
have a heat transfer coefficient of at least about 150 W/(m.sup.2
K), at least about 200 W/(m.sup.2 K), at least about 500 W/(m.sup.2
K), at least about 1000 W/(m.sup.2 K), at least about 2000
W/(m.sup.2 K), at least about 3000 W/(m.sup.2 K), at least about
4000 W/(m.sup.2 K), or, in some cases, at least about 5000
W/(m.sup.2 K). In some embodiments, the heat exchanger may have a
heat transfer coefficient in the range of at least about 150
W/(m.sup.2 K) to at least about 5000 W/(m.sup.2 K), at least about
200 W/(m.sup.2 K) to about 5000 W/(m.sup.2 K), at least about 500
W/(m.sup.2 K) to about 5000 W/(m.sup.2 K), at least about 1000
W/(m.sup.2 K) to about 5000 W/(m.sup.2 K), at least about 2000
W/(m.sup.2 K) to about 5000 W/(m.sup.2 K), at least about 3000
W/(m.sup.2 K) to about 5000 W/(m.sup.2 K), or at least about 4000
W/(m.sup.2 K) to about 5000 W/(m.sup.2 K).
In some embodiments, the heat exchanger may lower the temperature
of the condenser liquid outlet stream and/or other fluids flowing
through the heat exchanger. For example, the difference between the
temperature of a fluid entering the heat exchanger in conduit 306
or 310 and the fluid exiting the heat exchanger via conduit 308 or
312, respectively, may be at least about 5.degree. C., at least
about 10.degree. C., at least about 15.degree. C., at least about
20.degree. C., at least about 30.degree. C., at least about
40.degree. C., at least about 50.degree. C., at least about
60.degree. C., at least about 70.degree. C., at least about
80.degree. C., at least about 90.degree. C., at least about
100.degree. C., at least about 150.degree. C., or, in some cases,
at least about 200.degree. C. In some embodiments, the difference
between the temperature of a fluid entering the heat exchanger and
the fluid exiting the heat exchanger may be in the range of about
5.degree. C. to about 30.degree. C., about 5.degree. C. to about
60.degree. C., about 5.degree. C. to about 90.degree. C., about
10.degree. C. to about 30.degree. C., about 10.degree. C. to about
60.degree. C., about 10.degree. C. to about 90.degree. C., about
20.degree. C. to about 60.degree. C., about 20.degree. C. to about
90.degree. C., about 20.degree. C. to about 200.degree. C., about
30.degree. C. to about 60.degree. C., about 30.degree. C. to about
90.degree. C., about 40.degree. C. to about 200.degree. C., about
60.degree. C. to about 90.degree. C., about 60.degree. C. to about
200.degree. C., about 80.degree. C. to about 200.degree. C., about
100.degree. C. to about 200.degree. C., or about 150.degree. C. to
about 200.degree. C.
In some embodiments, an optional external heating device may be
arranged in fluid communication with the bubble column condenser
and/or the external heat exchanger. In certain cases, the heating
device may be arranged such that, in operation, a condenser liquid
outlet stream is heated in the heating device prior to entering the
heat exchanger. Such an arrangement may advantageously increase the
amount of heat transferred from the condenser liquid outlet stream
to another fluid stream flowing through the heat exchanger. For
example, in a humidification-dehumidification system, heat may be
transferred from the condenser liquid outlet stream to a
salt-containing water stream (e.g., a brine stream) prior to entry
of the salt-containing water stream into a humidifier.
The heating device may be any device that is capable of
transferring heat to a fluid stream (e.g., a condenser liquid
outlet stream). In some cases, the heating device is a heat
exchanger. Any heat exchanger known in the art may be used.
Examples of suitable heat exchangers include, but are not limited
to, plate and frame heat exchangers, shell and tube heat
exchangers, tube and tube heat exchangers, plate heat exchangers,
plate and shell heat exchangers, and the like. In a particular
embodiment, the heat exchanger is a plate and frame heat exchanger.
The heat exchanger may be configured such that a first fluid stream
and a second fluid stream flow through the heat exchanger. In some
cases, the first fluid stream and the second fluid stream may flow
in substantially the same direction (e.g., parallel flow),
substantially opposite directions (e.g., counter flow), or
substantially perpendicular directions (e.g., cross flow). The
first fluid stream and/or the second fluid stream may comprise a
liquid. In some embodiments, the second heat exchanger is a
liquid-to-liquid heat exchanger. The first fluid stream may, in
some cases, comprise a fluid stream that flows through a condenser
(e.g., a condenser liquid outlet stream). The second fluid stream
may, in some cases, comprise a heating fluid. The second fluid
stream may, in some cases, comprise a heating fluid. The heating
fluid may be any fluid capable of absorbing and transferring heat.
In some embodiments, the heating fluid comprises water. In certain
cases, the heating fluid comprises hot, pressurized water. In
certain embodiments, heat may be transferred from the second fluid
stream (e.g., the heating fluid) to the first stream (e.g., the
condenser liquid outlet stream) in the heat exchanger. In some
cases, more than two fluid streams may flow through the heat
exchanger.
In some embodiments, the heating device is a heat collection
device. The heat collection device may be configured to store
and/or utilize thermal energy (e.g., in the form of combustion of
natural gas, solar energy, waste heat from a power plant, or waste
heat from combusted exhaust). In certain cases, the heating device
is configured to convert electrical energy to thermal energy. For
example, the heating device may be an electric heater.
The heating device may, in some cases, increase the temperature of
the condenser liquid outlet stream and/or other fluid streams
flowing through the heating device. For example, the difference
between the temperature of a fluid entering the heating device and
the fluid exiting the heating device may be at least about
5.degree. C., at least about 10.degree. C., at least about
15.degree. C., at least about 20.degree. C., at least about
30.degree. C., at least about 40.degree. C., at least about
50.degree. C., at least about 60.degree. C., at least about
70.degree. C., at least about 80.degree. C., or, in some cases, at
least about 90.degree. C. In some embodiments, the difference
between the temperature of a fluid entering the heating device and
the fluid exiting the heat exchanger may be in the range of about
5.degree. C. to about 30.degree. C., about 5.degree. C. to about
60.degree. C., about 5.degree. C. to about 90.degree. C., about
10.degree. C. to about 30.degree. C., about 10.degree. C. to about
60.degree. C., about 10.degree. C. to about 90.degree. C., about
20.degree. C. to about 60.degree. C., about 20.degree. C. to about
90.degree. C., about 30.degree. C. to about 60.degree. C., about
30.degree. C. to about 90.degree. C., or about 60.degree. C. to
about 90.degree. C. In some cases, the temperature of a fluid
stream (e.g., the condenser liquid outlet stream) being heated in
the heating device remains below the boiling point of the fluid
stream.
In some embodiments, an optional external cooling device may be
arranged in fluid communication with the bubble column condenser
and/or the external heat exchanger. In certain cases, the cooling
device may be arranged such that, in operation, a heat exchanger
outlet stream (e.g., a cooled condenser liquid outlet stream) is
cooled in the cooling device prior to returning to the bubble
column condenser.
A cooling device generally refers to any device that is capable of
removing heat from a fluid stream (e.g., a liquid stream, a gas
stream). In some embodiments, the cooling device is a heat
exchanger. The heat exchanger may be configured such that a first
fluid stream and a second fluid stream flow through the heat
exchanger. In some cases, the first fluid stream and the second
fluid stream may flow in substantially the same direction (e.g.,
parallel flow), substantially opposite directions (e.g., counter
flow), or substantially perpendicular directions (e.g., cross
flow). In some cases, heat is transferred from a first fluid stream
to a second fluid stream. In certain embodiments, the cooling
device is a liquid-to-gas heat exchanger. The first fluid stream
may, in certain cases, comprise a fluid stream that is part of a
loop of condenser liquid flowing between a condenser and a heat
exchanger (e.g., a condenser liquid outlet stream). The second
fluid stream may, in some cases, comprise a coolant. The coolant
may be any fluid capable of absorbing or transferring heat. In some
embodiments, the coolant comprises a gas. The gas may, in some
cases, comprise air (e.g., ambient air). Heat exchangers that
comprise air as a coolant may generally be referred to as
air-cooled heat exchangers. In some cases, more than two fluid
streams flow through the cooling device. It should also be noted
that the cooling device may, in some embodiments, be a dry cooler,
a chiller, a radiator, or any other device capable of removing heat
from a fluid stream.
The cooling device may, in some cases, decrease the temperature of
a heat exchanger outlet stream. In some embodiments, the cooling
device decreases the temperature of the heat exchanger outlet
stream by at least about 5.degree. C., at least about 10.degree.
C., at least about 15.degree. C., at least about 20.degree. C., at
least about 30.degree. C., at least about 40.degree. C., at least
about 50.degree. C., at least about 60.degree. C., at least about
70.degree. C., at least about 80.degree. C., or, in some cases, at
least about 90.degree. C. In some embodiments, the cooling device
decreases the temperature of the heat exchanger outlet stream by an
amount in the range of about 5.degree. C. to about 30.degree. C.,
about 5.degree. C. to about 60.degree. C., about 5.degree. C. to
about 90.degree. C., about 10.degree. C. to about 30.degree. C.,
about 10.degree. C. to about 60.degree. C., about 10.degree. C. to
about 90.degree. C., about 20.degree. C. to about 30.degree. C.,
about 20.degree. C. to about 60.degree. C., about 20.degree. C. to
about 90.degree. C., about 30.degree. C. to about 60.degree. C.,
about 30.degree. C. to about 90.degree. C., or about 60.degree. C.
to about 90.degree. C.
FIG. 3B shows an exemplary embodiment of a system 300 comprising a
bubble column condenser 302, an external heat exchanger 304, an
external heating device 314, and an external cooling device 316,
each in fluid communication with one another. Heating device 314 is
arranged to be in fluid communication with condenser 302 via liquid
conduit 306. Heating device 314 is also arranged to be in fluid
communication with heat exchanger 304 via liquid conduit 318. In
addition to being in fluid communication with heating device 314,
heat exchanger 304 is arranged to be in fluid communication with
cooling device 316 via liquid conduit 320. Cooling device 316 is
arranged to be in fluid communication with condenser 302 via liquid
conduit 308.
In operation, in an exemplary embodiment, a condenser liquid outlet
stream exits condenser 302 via conduit 306 at a temperature T.sub.1
and enters heating device 314. Heat is transferred to the condenser
liquid outlet stream as it flows through heating device 314. The
condenser liquid outlet stream exits heating device 314 as a
heating device outlet stream (e.g., a heated condenser liquid
outlet stream) at a temperature T.sub.2 that is higher than
T.sub.1. The heating device outlet stream then flows through
conduit 318 to heat exchanger 304. In heat exchanger 304, heat is
transferred from the heating device outlet stream to another fluid
stream (e.g., a salt-containing water stream) flowing through heat
exchanger 304 via conduits 310 and 312. The heating device outlet
stream exits heat exchanger 304 as a heat exchanger outlet stream
at a temperature T.sub.3 that is lower than T.sub.2. The heat
exchanger outlet stream then flows through liquid conduit to
cooling device 316. In some embodiments, as the heat exchanger
outlet stream flows through cooling device 316, heat from the heat
exchanger outlet stream is transferred to another fluid stream
(e.g., an air stream) flowing through cooling device 316 via
conduits 322 and 324. The heat exchanger outlet stream then exits
cooling device 316 as a cooling device outlet stream at a
temperature T.sub.4 that is lower than T.sub.3. The cooling device
outlet stream at temperature T.sub.4 then returns to condenser 302
via conduit 308.
In some embodiments, the bubble column condenser may be used in a
desalination system. In some embodiments, the desalination system
may be a humidification-dehumidification (HDH) system. In such
systems, a condenser (e.g., bubble column condenser) may act as a
dehumidifier to condense substantially purified water from a
humidified gas stream. Use of a bubble column condenser as a
dehumidifier in an HDH system may be advantageous because direct
contact condensers, such as bubble column condensers, may exhibit
relatively higher heat transfer effectiveness than other types of
condensers, such as surface condensers. In some embodiments, the
HDH system comprises a heat exchanger. In certain cases, the heat
exchanger facilitates the transfer of heat from a fluid stream
flowing through a condenser (e.g., a condenser liquid outlet
stream) to a fluid stream flowing through a humidifier (e.g., a
humidifier liquid inlet stream). For example, the heat exchanger
may advantageously allow energy to be recovered from a condenser
liquid outlet stream and used to pre-heat a humidifier liquid inlet
stream (e.g., a salt-containing water stream) prior to entry of the
humidifier liquid inlet stream into the humidifier of the HDH
system. This may, for example, avoid the need for an additional
heating device to heat the salt-containing water stream.
Alternatively, if a heating device is used, the presence of a heat
exchanger to recover energy from a condenser liquid outlet stream
may reduce the amount of heat required to be applied to the
salt-containing water stream. In some embodiments, the heat
exchanger is an external heat exchanger. As noted above, the use of
an external heat exchanger may advantageously allow the use of
bubble column condensers as described herein (e.g., condensers
having reduced dimensions and/or reduced levels of liquid baths,
etc.). In some embodiments, the heat exchanger is an internal heat
exchanger. For example, the internal heat exchanger may comprise a
tube coil located within a bubble column condenser. The tube coil
may be positioned such that at least a portion of the tube coil is
in thermal contact with a liquid layer within a stage of the bubble
column condenser. In a multi-stage bubble condenser comprising a
plurality of stages, each stage comprising a liquid layer, the tube
coil may be positioned such that each liquid layer is in thermal
contact with at least a portion of the tube coil. In some cases, a
coolant (e.g., a salt-containing water stream) may flow through the
internal heat exchanger (e.g., the tube coil), and heat may be
transferred from the liquid layer(s) of the bubble column condenser
to the coolant.
Other examples of HDH systems are described in U.S. Pat. No.
8,292,272, by Elsharqawy et al., filed Sep. 4, 2009, entitled
"Water Separation Under Reduced Pressure"; U.S. Pat. No. 8,465,006,
by Elsharqawy et al., filed Sep. 21, 2012, entitled "Separation of
a Vaporizable Component Under Reduced Pressure"; U.S. Pat. No.
8,252,092, by Govindan et al., filed Oct. 5, 2009, entitled "Water
Separation Under Varied Pressure"; U.S. Pat. No. 8,496,234, by
Govindan et al., filed Jul. 16, 2012, entitled "Thermodynamic
Balancing of Combined Heat and Mass Exchange Devices"; U.S. Patent
Publication No. 2013/0074694, by Govindan et al., filed Sep. 23,
2011, entitled "Bubble-Column Vapor Mixture Condenser"; U.S. Patent
Publication No. 2013/0075940, by Govindan et al., filed Jul. 12,
2012 as U.S. patent application Ser. No. 13/548,166, entitled
"Bubble-Column Vapor Mixture Condenser"; and U.S. patent
application Ser. No. 13/916,038, by Govindan et al., filed Jun. 12,
2013, entitled "Multi-Stage Bubble Column Humidifier," the contents
of which are incorporated herein by reference in their entireties
for all purposes.
An exemplary embodiment of an HDH system is shown in FIG. 4A.
System 400 includes a humidifier 402, a dehumidifier 404, a heat
exchanger 406, a reservoir of salt-containing water 408, and a
reservoir of purified water 410. Humidifier 402 and dehumidifier
404 are arranged in fluid communication via gas conduits 420 and
422. In some embodiments, system 400 is a closed loop system, with
a carrier gas stream circulating between humidifier 402 and
dehumidifier 404. In some cases, the carrier gas stream may
comprise a non-condensable gas. In addition to the carrier gas
stream, various liquid streams are circulated through system 400.
In one case, the stream may include salt-containing water, such as
seawater, brackish water, saline water, brine, and/or industrial
wastewater. In system 400, a reservoir of salt-containing water 408
is arranged in fluid communication with heat exchanger 406 via
liquid conduit 412 and with humidifier 402 through liquid conduit
418. Humidifier 402 is also arranged to be in fluid communication
with heat exchanger 406 via liquid conduits 414 and 416. In some
embodiments, humidifier 402 may comprise a humidifier liquid inlet
and outlet and a humidifier gas inlet and outlet. In some cases,
the humidifier is configured such that the liquid inlet is
positioned at a first end (e.g., top end) of the humidifier, and
the gas inlet is positioned at a second, opposite end (e.g., bottom
end) of the humidifier. Such a configuration may advantageously
result in high thermal efficiency. In some embodiments, the
humidifier is configured to bring a carrier gas stream (e.g., dry
air) into direct contact with a salt-containing water stream,
thereby producing a vapor-containing humidifier gas outlet stream
enriched in water relative to the gas received from the humidifier
gas inlet. Humidifier 402 may also produce a humidifier liquid
outlet stream, a portion of which is returned to reservoir 408 and
a portion of which is flowed through heat exchanger 406 to be
heated and reintroduced to the humidifier. Any humidifier known to
those of ordinary skill in the art may be utilized in the context
of the embodiments described herein. According to certain
embodiments, the humidifier may be a packed bed humidifier. For
example, in some such embodiments, humidification of the carrier
gas may be achieved by spraying salt-containing water from one or
more nozzles located at the top of the humidifier through a packing
material (e.g., a polyvinyl chloride packing material or a
glass-filled polypropylene packing material) while the carrier gas
travels through the humidification chamber and is brought into
contact with the salt-containing water. In some embodiments, the
packing material may increase the surface area of the
salt-containing water stream that is contact with the carrier gas,
thereby increasing the portion of water that is vaporized into the
carrier gas. In some embodiments, the humidifier may be a bubble
column humidifier. It has been recognized that use of a bubble
column humidifier may, in some cases, be preferable to use of other
types of bubble column humidifiers (e.g., packed bed humidifiers).
For example, bubble column humidifiers may be characterized by
improved performance (e.g., higher rates of heat and/or mass
transfer, higher thermodynamic effectiveness) and/or reduced
fabrication and/or material costs (e.g., reduced dimensions).
In some embodiments, dehumidifier 404 is a bubble column condenser
as described herein. In some embodiments, condenser 404 is in fluid
communication with reservoir 410 through conduit 430. Condenser 404
may also be in fluid communication with heat exchanger 406 via
conduits 426 and 428. Heat exchanger 406 may be any heat exchanger
known in the art, as described elsewhere herein. In some
embodiments the heat exchanger is configured such that a first
fluid stream and a second fluid stream flow through the heat
exchanger in substantially opposite direction (e.g., counter flow).
For example, FIG. 4B shows heat exchanger 406 as a counter flow
device. The heat exchanger may, alternatively, be a parallel flow
device and may be configured such that a first fluid stream and a
second fluid stream flow in substantially the same direction. FIG.
4A shows heat exchanger 406 as a parallel flow device. In some
embodiments, the heat exchanger is a cross flow device, and the
heat exchanger is configured such that a first fluid stream and a
second fluid stream flow in substantially perpendicular directions.
In some cases, the heat exchanger is a liquid-to-liquid heat
exchanger. In an exemplary embodiment, the heat exchanger is a
plate and frame heat exchanger. In certain embodiments, heat
exchanger 406 is in fluid communication with reservoir 410 via
optional conduit 424. In operation, in the exemplary embodiment
shown in FIG. 4A, a salt-containing water stream flows from
reservoir 408 to heat exchanger 406 via conduit 412 to be heated
prior to entering humidifier 402 (e.g., "preheated"). The preheated
salt-containing water stream then travels from heat exchanger 406
through conduit 414 to humidifier 402. In some cases, a first
portion of the preheated salt-containing water stream flows from
heat exchanger 406 to humidifier 402, and, optionally, a second
portion of the preheated salt-containing water stream is discharged
from the system and/or routed to another portion of the system.
Separately, and in a direction that is opposite to the direction of
flow for the preheated salt-containing water stream, a carrier gas
stream provided by condenser 404 is flowed through humidifier 402.
In humidifier 402, the carrier gas stream, which is at a
temperature that is lower than the preheated salt-containing water
stream, is heated and humidified by the preheated salt-containing
water stream. The humidified carrier gas stream exits humidifier
402 and flows through gas conduit 420 to dehumidifier 404. A
portion of the salt-containing water stream returns to reservoir
408 via conduit 418, and a portion flows through liquid conduit 416
to heat exchanger 406 to be preheated before being returned to
humidifier 402 via liquid conduit 414.
The humidified carrier gas stream is then flowed through bubble
column condenser 404. Flowing countercurrent to the humidified
carrier gas stream in the bubble column condenser is a condenser
liquid stream that flows from heat exchanger 406 to bubble column
condenser 404 through conduit 426. In some embodiments, the
condenser liquid stream comprises purified water, which may be
substantially pure water. In some cases, a first portion of the
condenser liquid stream that has flowed through heat exchanger 406
is flowed to bubble column condenser 404 and, optionally, a second
portion of the condenser liquid stream that has flowed through heat
exchanger 406 is discharged from the system and/or routed to
another portion of the system. In some cases in which a portion of
the condenser liquid stream is discharged from the system, the rate
that the liquid stream is discharged is about the same as the rate
that the liquid is being condensed, in order to maintain a constant
volume of water in the system. In bubble column condenser 404, the
humidified carrier gas stream undergoes a condensation process as
described elsewhere herein, wherein heat and mass are transferred
from the humidified carrier gas stream to the condenser liquid
stream, producing a dehumidified carrier gas stream and a condenser
liquid outlet stream. The dehumidified gas stream is returned to
humidifier 402 via gas conduit 422 for use as described herein. In
some embodiments, a portion of the condenser liquid outlet stream
is flowed through liquid conduit 430 to reservoir 410. The purified
water that is collected in reservoir 410 can be used, for example,
for drinking, watering crops, washing/cleaning, cooking, for
industrial use, etc. The remaining portion of the condenser liquid
outlet stream that is not flowed to reservoir 410 is returned to
heat exchanger 406 via liquid conduit 428. As described herein,
heat from the condenser liquid outlet stream may be transferred to
the salt-containing water stream flowing through liquid conduits
412, 414, and 416. After flowing through heat exchanger 406, the
condenser liquid outlet stream then flows through liquid conduit
426 and returns to condenser 404 for reuse.
In some embodiments, an HDH system optionally comprises one or more
heating devices. An exemplary embodiment of an HDH system
comprising two heating devices is shown in FIG. 4C. In FIG. 4C,
first heating device 432 is arranged to be in fluid communication
with heat exchanger 406 via liquid conduit 436 and in fluid
communication with humidifier 402 via liquid conduit 414. Second
heating device 434 is arranged to be in fluid communication with
heat exchanger 406 via liquid conduit 438 and condenser 404 via
liquid conduit 428. The first heating device and second heating
device may be any device that is capable of transferring heat to a
fluid stream. In some embodiments, the first and/or second heating
device is a heat exchanger. The heat exchanger may be any heat
exchanger known in the art, as described elsewhere herein (e.g., a
plate and frame heat exchanger). In some embodiments, the first
and/or second heating device is a heat collection device. In some
cases, the heat collection device may be configured to store and/or
utilize thermal energy (e.g., in the form of combustion of natural
gas, solar energy, waste heat from a power plant, or waste heat
from combusted exhaust). In certain cases, the heating device is
configured to convert electrical energy to thermal energy (e.g., an
electric heater).
The first and/or second heating device may, in some cases, increase
the temperature of a fluid stream flowing through the first and/or
second heating device. For example, the difference between the
temperature of a fluid stream entering the first and/or second
heating device and the fluid stream exiting the first and/or second
heating device may be at least about 5.degree. C., at least about
10.degree. C., at least about 15.degree. C., at least about
20.degree. C., at least about 30.degree. C., at least about
40.degree. C., at least about 50.degree. C., at least about
60.degree. C., at least about 70.degree. C., at least about
80.degree. C., or, in some cases, at least about 90.degree. C. In
some embodiments, the difference between the temperature of a fluid
stream entering the first and/or second heating device and the
fluid stream exiting the first and/or second heating device may be
in the range of about 5.degree. C. to about 30.degree. C., about
5.degree. C. to about 60.degree. C., about 5.degree. C. to about
90.degree. C., about 10.degree. C. to about 30.degree. C., about
10.degree. C. to about 60.degree. C., about 10.degree. C. to about
90.degree. C., about 20.degree. C. to about 60.degree. C., about
20.degree. C. to about 90.degree. C., about 30.degree. C. to about
60.degree. C., about 30.degree. C. to about 90.degree. C., or about
60.degree. C. to about 90.degree. C.
In operation, a salt-containing water stream may first flow through
heat exchanger 406. In heat exchanger 406, heat may be transferred
from another fluid stream (e.g., a condenser liquid stream) to the
salt-containing water stream, resulting in a heated salt-containing
water stream. The heated salt-containing water stream may then be
flowed through liquid conduit 436 to first heating device 432 to be
heated, resulting in a further heated salt-containing water stream.
The further heated salt-containing water stream may then be flowed
to humidifier 402.
In the opposite direction, a condenser liquid stream exiting
dehumidifier 404 may flow through liquid conduit 428 to second
heating device 434 to be heated, resulting in a heated condenser
liquid stream. The heated condenser liquid stream may then be
directed to flow through liquid conduit 438 to heat exchanger 406,
and heat may be transferred from the heated condenser liquid stream
to the salt-containing water stream, resulting in a chilled
condenser liquid stream. The chilled condenser liquid stream may
then be returned to condenser 404 through liquid conduit 426.
It should be noted that although FIG. 4C shows a first heating
device and a second heating device, the first and second heating
devices may independently be present or absent in an HDH system. In
some embodiments, a first heating device further heats a
salt-containing water stream after the stream has flowed through a
heat exchanger. In some embodiments, a second heating device heats
a condenser liquid stream prior to the stream flowing through the
heat exchanger. In some cases, the first heating device heats the
salt-containing water stream and the second heating device heats
the condenser liquid stream. In some embodiments, a single heating
device may function as the first heating device and second heating
device and heat both the salt-containing water stream and the
condenser liquid stream. Further, there may be any number of
heating devices present in HDH system 400.
The humidifier may, in some cases, be substantially thermally
separated from the bubble column condenser. As used herein,
substantial thermal separation generally refers to a configuration
such that there is little to no direct conductive heat transfer
between the humidifier and the bubble column condenser, for example
through a shared heat transfer wall. However, it should be
understood that such a configuration does not preclude a mass flow
carrying thermal energy (via gas and/or liquid flow) between the
humidifier and the condenser.
Those of ordinary skill in the art would be able to select the
appropriate conditions under which to operate the HDH systems
described herein for desired performance given the teaching and
guidance of the present specification combined with the knowledge
and skill of the person of ordinary skill in the art. In some
embodiments, the pressure in the humidification and/or
dehumidification chamber is approximately ambient atmospheric
pressure. According to certain embodiments, the pressure in the
humidification and/or dehumidification chamber is less than about
90,000 Pa. It may be desirable, in some embodiments, for the
pressure in the humidifier to be less than approximately ambient
atmospheric pressure. In some cases, as the pressure inside the
humidifier decreases, the ability of the humidified carrier gas to
carry more water vapor increases, allowing for increased production
of substantially pure water when the carrier gas is dehumidified in
the condenser. Without wishing to be bound by a particular theory,
this effect may be explained by the humidity ratio, which generally
refers to the ratio of water vapor mass to dry air mass in moist
air, being higher at pressures lower than atmospheric pressure.
Those of ordinary skill in the art would be able to select
appropriate temperature and flow rate conditions for the HDH system
components. In some embodiments, the selected conditions may be
within the ranges described herein for the bubble column
condenser.
According to some embodiments, a portion of the gas flow is
extracted from at least one intermediate location in the humidifier
and injected into at least one intermediate location in the bubble
column condenser. Because the portion of the gas flow exiting the
humidifier at an intermediate outlet (e.g., the extracted portion)
has not passed through the entire humidifier, the temperature of
the gas flow at the intermediate outlet may be lower than the
temperature of the gas flow at the main gas outlet of the
humidifier. The location of the extraction points (e.g., outlets)
and/or injection points (e.g., inlets) may be selected to increase
the thermal efficiency of the system. For example, because a gas
(e.g., air) may have increased vapor content at higher temperatures
than at lower temperatures, and because the heat capacity of a gas
with higher vapor content may be higher than the heat capacity of a
gas with lower vapor content, less gas may be used in higher
temperature areas of the humidifier and/or bubble column condenser
to better balance the heat capacity rate ratios of the gas (e.g.,
air) and liquid (e.g., water) streams. Extraction and/or injection
at intermediate locations may advantageously allow for manipulation
of gas mass flows and for greater heat recovery. For example, a 30%
intermediate extraction at 160.degree. F. from a humidifier with a
top moist air temperature of 180.degree. F. and injection after the
second stage in an 8-stage bubble column can reduce energy
consumption by about 40% to about 50%.
It should be recognized that in some embodiments, under some
operating conditions, extraction may not increase the thermal
efficiency of an HDH system. Additionally, there may be drawbacks
associated with extraction at intermediate locations. For example,
extraction may reduce the water production rate of the system, and
there may be significant monetary costs associated with extraction
(e.g., costs associated with instrumentation, ducting, insulation,
and/or droplet separation). Accordingly, in some cases, it may be
advantageous to build and/or operate a system without
extraction.
In some embodiments, the HDH system further comprises an optional
cooling device. The cooling device may be any device that is
capable of removing heat from a fluid stream, as described
elsewhere herein. In some embodiments, the cooling device is a heat
exchanger. The heat exchanger may be configured such that a first
fluid stream and a second fluid stream flow through the heat
exchanger. In some cases, the first fluid stream and the second
fluid stream may flow in substantially the same direction (e.g.,
parallel flow), substantially opposite directions (e.g., counter
flow), or substantially perpendicular directions (e.g., cross
flow). In some cases, heat is transferred from a first fluid stream
to a second fluid stream. In certain embodiments, the cooling
device is a liquid-to-gas heat exchanger. The first fluid stream
may, in certain cases, comprise a fluid stream that is part of a
loop of condenser liquid flowing between a condenser and a heat
exchanger (e.g., a condenser liquid outlet stream). The second
fluid stream may, in some cases, comprise a coolant. The coolant
may be any fluid capable of absorbing or transferring heat. In some
embodiments, the coolant comprises a gas. The gas may, in some
cases, comprise air (e.g., ambient air). Heat exchangers that
comprise air as a coolant may generally be referred to as
air-cooled heat exchangers. In some cases, more than two fluid
streams flow through the cooling device. It should also be noted
that the cooling device may, in some embodiments, be a dry cooler,
a chiller, a radiator, or any other device capable of removing heat
from a fluid stream.
In some cases, the presence of a cooling device in an HDH system
can advantageously increase the amount of water recovered in the
HDH system. In the absence of a cooling device, a fresh water
stream entering a dehumidifier may be cooled in a heat exchanger
through transfer of heat to a cooled salt-containing water stream.
In the absence of a cooling device, the temperature of the fresh
water stream flowing through a dehumidifier may therefore limited
by the temperature of the brine stream. In the presence of a
cooling device, the temperature of the fresh water entering the
dehumidifier may no longer be limited by the temperature of the
brine stream, and lower temperatures may be achieved. Since air can
generally hold less vapor at lower temperatures, more water may be
recovered at lower temperatures. In some cases, the cooling device
may increase water production by at least about 5%, at least about
10%, at least about 20%, at least about 30%, at least about 40%, or
at least about 50%. The inclusion of a cooling device may, in some
cases, advantageously increase water production with a minimal
concomitant increase in electricity consumption.
In some embodiments, one fluid stream flowing through the cooling
device is a condenser liquid stream. The condenser liquid stream
may, in some cases, comprise purified water, which may be
substantially pure water. For example, the condenser liquid stream
may comprise part of a loop of condenser liquid (e.g., purified
water) flowing between a condenser and a heat exchanger. In certain
embodiments, one fluid stream flowing through the cooling device
comprises air (e.g., ambient air). The cooling device may be
arranged, in some cases, such that the condenser liquid stream
flows through the cooling device after flowing through a heat
exchanger. In some cases, the cooling device may be arranged such
that the condenser liquid stream flows through the cooling device
before flowing through a dehumidifier (e.g., a bubble column
condenser).
In some cases, the cooling device decreases the temperature of the
condenser liquid stream. In some embodiments, the cooling device
decreases the temperature of the condenser liquid stream by at
least about 5.degree. C., at least about 10.degree. C., at least
about 15.degree. C., at least about 20.degree. C., at least about
30.degree. C., at least about 40.degree. C., at least about
50.degree. C., at least about 60.degree. C., at least about
70.degree. C., at least about 80.degree. C., or, in some cases, at
least about 90.degree. C. In some embodiments, the cooling device
decreases the temperature of the condenser liquid stream by an
amount in the range of about 5.degree. C. to about 30.degree. C.,
about 5.degree. C. to about 60.degree. C., about 5.degree. C. to
about 90.degree. C., about 10.degree. C. to about 30.degree. C.,
about 10.degree. C. to about 60.degree. C., about 10.degree. C. to
about 90.degree. C., about 20.degree. C. to about 60.degree. C.,
about 20.degree. C. to about 90.degree. C., about 30.degree. C. to
about 60.degree. C., about 30.degree. C. to about 90.degree. C., or
about 60.degree. C. to about 90.degree. C.
An exemplary embodiment of an HDH system comprising a cooling
device is shown in FIG. 9. In FIG. 9, HDH system 900 comprises a
humidifier 902, a dehumidifier 904, a first reservoir of
salt-containing water 906, a second reservoir of salt-containing
water 908, a reservoir of purified water 910, a heat exchanger 912,
an optional first heating device 914, an optional second heating
device 916, and a cooling device 918. Humidifier 902 and
dehumidifier 904 are arranged in fluid communication via gas
conduits 930 and 932. In addition to being in fluid communication
with dehumidifier 904, humidifier 902 is arranged to be in fluid
communication with second reservoir of salt-containing water 908
via liquid conduit 934. Humidifier 902 is also arranged to be in
fluid communication with heat exchanger 912 via liquid conduit 936
and optional first heating device 914 via liquid conduit 940.
Dehumidifier 904, in addition to being in fluid communication with
humidifier 902, is arranged to be in fluid communication with
reservoir of purified water 910 via liquid conduit 942, optional
second heating device 916 via liquid conduit 944, and cooling
device 918 via liquid conduit 950. Dehumidifier 904 may be a bubble
column condenser as described herein. In some embodiments, cooling
device 918 is arranged to be in fluid communication with heat
exchanger 912 via liquid conduit 948. Cooling device 918 is also
arranged to be in fluid communication with a gas stream (e.g., an
air stream) through gas conduits 952 and 954. First reservoir of
salt-containing water 906 is arranged to be in fluid communication
with heat exchanger 912 via liquid conduit 956. First reservoir of
salt-containing water 906 may also be fluidly connected to an
external source of salt-containing water (e.g., from oil and/or gas
production), not shown in FIG. 9.
In operation, a salt-containing water stream may flow from first
reservoir of salt-containing water 906 to heat exchanger 912. Heat
may be transferred from another fluid stream (e.g., a condenser
liquid stream) to the salt-containing water stream, resulting in a
heated salt-containing water stream. The heated salt-containing
water stream may then flow to optional first heating device 914 via
liquid conduit 938 to be further heated. The further heated
salt-containing water stream may be directed to flow to humidifier
902 via liquid conduit 940. In humidifier 902, at least a portion
of water may be evaporated to a carrier gas stream flowing through
humidifier 902 counterflow to the salt-containing water stream. A
first portion of the remaining salt-containing water that is not
evaporated may then flow to second salt-containing reservoir 908
via liquid conduit 934. A second portion of the remaining
salt-containing water that is not evaporated may be recirculated to
heat exchanger 912 via liquid conduit 936.
A carrier gas stream may flow in a direction opposite that of the
salt-containing water stream. The carrier gas stream may enter
humidifier 902 and come into contact with the heated
salt-containing water stream. Water may be evaporated to the
carrier gas stream, thereby resulting in a humidified carrier gas
stream. The humidified carrier gas stream may flow to dehumidifier
904 via gas conduit 930. In dehumidifier 904, the humidified
carrier gas stream may come into contact with a chilled condenser
liquid stream flowing in the opposite direction. Heat and mass may
be transferred from the humidified carrier gas stream to the
chilled condenser liquid stream as water is condensed from the
humidified carrier gas stream, resulting in a dehumidified carrier
gas stream. The dehumidified carrier gas stream may be flowed to
humidifier 902 via gas conduit 932.
A condenser fluid (e.g., water) stream may flow through
dehumidifier 904 counterflow to the carrier gas stream. As the
condenser fluid stream flows through dehumidifier 904, water may be
condensed from the humidified carrier gas stream to the condenser
liquid stream, thereby resulting in a condenser liquid outlet
stream. At least a portion of the condenser liquid outlet stream
may flow through liquid conduit 942 to reservoir of purified water
910. At least a portion of the condenser liquid outlet stream may
flow through optional second heating device 916 via liquid conduit
944. In optional second heating device 914, the condenser liquid
outlet stream may be heated, resulting in a heated condenser liquid
outlet stream. In some cases, the heated condenser liquid outlet
stream may flow to heat exchanger 912 via liquid conduit 946. In
heat exchanger 912, the heated condenser liquid outlet stream may
transfer heat to the salt-containing water stream, resulting in a
chilled condenser liquid outlet stream. The chilled condenser
liquid outlet stream may then flow to cooling device 918 via liquid
conduit 948. A gas stream may also flow through cooling device 918.
The two streams may flow parallel, counter flow, or cross flow to
each other. In some embodiments, the gas stream comprises air. The
air may, for example, enter cooling device 918 through gas conduit
952 and exit cooling device 918 through gas conduit 954. In some
embodiments, heat may be transferred from the chilled condenser
liquid outlet stream to the air, resulting in a further chilled
condenser liquid outlet stream. The further chilled condenser
liquid outlet stream may then be flowed to dehumidifier 904 through
liquid conduit 950.
Example 1
In the following example, an 8-stage bubble column condenser and a
heat exchanger for use in a humidification-dehumidification system
are described. As shown in FIG. 5, system 500 includes
custom-designed condenser 502 and heat exchanger 504 in fluid
communication with one another. The exterior of the condenser
comprises stainless steel, and the condenser has the shape of a
rectangular prism. Eight stages, as described herein, are arranged
vertically within the bubble condenser, with a sump volume 506
located beneath the stages in fluid communication with a liquid
outlet 508. Each stage comprises a sparger plate (1.8 m long, 0.6 m
wide, and 0.06 m tall, having a plurality of holes with a diameter
of about 0.003 m) and a chamber in which a liquid bath can reside.
A first gas inlet 510 is positioned below the sparger plate located
near the bottom of the bubble column condenser, and a second gas
inlet 512 is positioned at an intermediate location between. Above
the topmost stage, a liquid inlet 514 and a mist eliminator (e.g.,
droplet eliminator) 516 that is coupled to a first gas outlet 518
are arranged.
Bubble column condenser 502 is coupled to heat exchanger 504, which
has two conduits 520 and 522. First conduit 520 is fluidically
connected to liquid inlet 514 and outlet 508 of the bubble column
condenser. Second conduit 522 is fluidically connected to other
components of a humidification-dehumidification system.
When the humidification-dehumidification system (i.e., containing
the 8-stage bubble column condenser and heat exchanger as
described) is in operation, a first stream of dry air enters the
bubble column through first gas inlet 510 at a temperature of about
88.degree. C., 100% relative humidity, a volumetric flow rate of
4,992 cubic feet per minute (cfm), and a mass flow rate of 14,241
lbs/hr. A second stream of dry air enters the bubble column
condenser through second gas inlet 512 at a temperature of about
77.degree. C., 100% relative humidity, a volumetric flow rate of
1,697 cfm, and a mass flow rate of 5,777 lbs/hour. A liquid stream
enters the condenser at liquid inlet 514, at a temperature of about
45.degree. C., a volumetric flow rate of 187.6 gallons per minute
(gpm), and a mass flow rate of 93.8 lbs/hr. During operation, a gas
outlet stream and a liquid outlet stream are produced as described
herein. The gas outlet stream exits at gas outlet 518 at a
temperature of about 49.degree. C., a volumetric flow rate of about
3272 cfm, and a mass flow rate of 12,819 lbs/hr. The liquid outlet
stream exits the bubble column condenser and is pumped by a column
circulation pump 524 at a volumetric flow rate of 202 gallons per
minute and a mass flow rate of 101,064 lbs/hour. The liquid outlet
stream passes through one conduit of the heat exchanger. Heat is
transferred from the liquid outlet stream to a salt-containing
water stream flowing through conduit 522 of the heat exchanger
(e.g., the stream that is heated by the condenser liquid outlet
stream in the heat exchanger). The salt-containing water stream
enters the heat exchanger at about 42.degree. C., a volumetric flow
rate of 196.3 GPM, and a mass flow rate of 118,703 lbs/hr, and
leaves at about 81.degree. C., a volumetric rate of 196.3 GPM, and
a mass flow rate of 118,703 lbs/hr. A portion of the liquid outlet
stream is directed to a substantially pure water reservoir via
valve 526 at a temperature of about 45.degree. C., a volumetric
flow rate of 14.58 gallons per minute, and a mass flow rate of
about 7,289 lbs/hr. The remaining portion of the liquid outlet
stream returns to condenser 502 through liquid inlet 514. While the
system is undergoing substantially continuous operation, each stage
of the bubble column condenser contains about 0.1 m or less of
water.
Table 1 lists the constituents of a salt-containing water stream
prior to and after treatment (e.g., desalination) using the
humidification-dehumidification system described in this Example.
It is noted that the concentrations of calcium and magnesium
appeared to increase after treatment. This may be due to the bubble
column initially being supplied with local drinking water (e.g.,
from Midland, Tex.). The local drinking water was hard and had
relatively high concentrations of calcium and magnesium. As a
result, trace amounts of calcium and/or magnesium may have remained
in the bubble column during testing, and trace amounts of the
elements may have been present in the desalination effluent (e.g.,
the water stream after treatment). In contrast, pretreatment
systems upstream of the desalination system may have removed almost
all of the calcium and magnesium from the feed water stream (e.g.,
the water stream before treatment). Accordingly, the water stream
after treatment may have contained higher concentrations of calcium
and magnesium than the water stream before treatment.
An additional exemplary embodiment of an 8-stage bubble column
condenser is shown in FIG. 7. In FIG. 7A, bubble column condenser
700 comprises gas inlets 702 and 704, gas outlet 706, and liquid
inlet 708. FIG. 7B shows another view of condenser 700, which
comprises eight stages as described herein. FIGS. 7C-I show
additional views of the bubble column condenser and its
components.
TABLE-US-00001 TABLE 1 Salt-containing water profile before and
after treatment (i.e., desalination). Concentration Before
Concentration After Constituent Treatment Treatment Oil and Grease
ND ND Total Suspended Solids 57 mg/L ND Total Dissolved Solids
28,400 mg/L 35 mg/L Barium .701 mg/L .005 mg/L Bromide 1050 mg/L
1.16 mg/L Calcium ND 7.08 mg/L Chloride 13,300 mg/L 5.0 mg/L
Sulfate 1020 mg/L 5.1 mg/L Magnesium ND 0.775 mg/L Aluminum 37.5
mg/L 0.077 mg/L Sodium 11,800 mg/L 3.09 mg/L Strontium 67 mg/L
0.079 ppm Zinc ND ND Benzene 37.5 ug/L ND Toluene 32.1 ug/L ND
Alkalinity (CaCO3) 3260 mg/L ND Recovery Ratio -- 82% (ND = Not
determinable)
Example 2
In this example, an 8-stage bubble column condenser and an external
heat exchanger for use in a humidification-dehumidification system
are described.
As shown in FIG. 10A, system 1000 comprised an 8-stage bubble
column condenser 1002 and a heat exchanger 1004, which were in
fluid communication with each other. Condenser 1002 and heat
exchanger 1004 were also in fluid communication with a humidifier
(not shown). In condenser 1002, eight stages 1002A, 1002B, 1002C,
1002D, 1002E, 1002F, 1002G, and 1002H were arranged vertically
within the condenser. Above topmost stage 1002A, a liquid inlet
1006 and a gas outlet 1022 were arranged. A sump volume 1002I was
located at the bottom of condenser 1002, beneath the bottommost
stage. Sump volume 1002I was in fluid communication with a liquid
outlet 1008. In addition, condenser 1002 further comprised a first
gas inlet 1018 positioned near the bottom of condenser 1002 and a
second gas inlet 1020 positioned at an intermediate location,
between the top and bottom of condenser 1002.
In operation, a stream of substantially pure water entered
condenser 1002 through liquid inlet 1006 and flowed downward
through each stage of condenser 1002. A stream of humidified
carrier gas flowed counterflow to the substantially pure water
stream, entering condenser 1002 through gas inlets 1018 and 1020
and flowing upwards through condenser 1002. As the two streams
flowed through condenser 1002, heat and mass were transferred from
the humidified carrier gas stream to the substantially pure water
stream. As a result, the temperature of the substantially pure
water stream increased as it flowed through each stage. In
uppermost stage 1002A, the temperature of the water stream was
141.6.degree. F. The temperature in stage 1002B was 148.3.degree.
F., the temperature in stage 1002C was 154.7.degree. F., the
temperature in stage 1002D was 161.5.degree. F., the temperature in
stage 1002E was 166.8.degree. F., the temperature in 1002F was
170.1.degree. F., the temperature in stage 1002G was 172.1.degree.
F., and the temperature in stage 1002H was 172.8.degree. F. Sump
volume 1002I, located at the bottom of condenser 1002, had 7.7
inches of water. The substantially pure water stream then exited
condenser 1002 through liquid outlet 1008 at a temperature of
173.4.degree. F.
As the substantially pure water stream exited condenser 1002, a
pump (not shown) operating at 68.6% capacity pumped the water
stream to heat exchanger 1004 at a volumetric flow rate of 180.8
gallons per minute. As the substantially pure water stream flowed
through heat exchanger 1004, heat was transferred from the
substantially pure water stream to another fluid stream flowing
through heat exchanger 1004, and the temperature of the
substantially pure water stream was reduced from 173.4.degree. F.
to 142.7.degree. F. After flowing through heat exchanger 1004 and
becoming chilled, a first portion of the chilled substantially pure
water stream was flowed through liquid conduit 1012 to a purified
water reservoir (not shown), and a second portion of the chilled
substantially pure water stream returned to condenser 1002 via
conduit 1010 through liquid inlet 1006.
In heat exchanger 1004, a salt-containing water stream was flowed
counterflow to the substantially pure water stream. Initially, the
salt-containing water stream flowed from a source of
salt-containing water through liquid conduit 1014. As it entered
heat exchanger 1004, the salt-containing water stream was at a
temperature of 121.3.degree. F. and a pressure of 43.4 psi. After
flowing through heat exchanger 1004 and receiving heat transferred
from the substantially pure water stream, the temperature of the
salt-containing water stream increased to 165.0.degree. F. The
pressure of the salt-containing water stream was 40.1 psi. The
heated salt-containing water stream was then flowed to the
humidifier.
Example 3
This example describes the 8-stage bubble column condenser and
external heat exchanger of Example 2, with the addition of an
external cooling device.
As shown in FIG. 10B, system 1000 comprised all the components
shown in FIG. 10A and further comprised an external cooling device
1024 in fluid communication with bubble column condenser 1002 and
heat exchanger 1004.
In operation, a stream of substantially pure water entered
condenser 1002 through liquid inlet 1006 and flowed downward
through each stage of condenser 1002. A stream of humidified
carrier gas flowed counterflow to the substantially pure water
stream, entering condenser 1002 through gas inlets 1018 and 1020
and flowing upwards through condenser 1002. As the two streams
flowed through condenser 1002, heat and mass were transferred from
the humidified carrier gas stream to the substantially pure water
stream. As a result, the temperature of the substantially pure
water stream increased as it flowed through each stage. In
uppermost stage 1002A, the temperature of the water stream was
124.8.degree. F. The temperature in stage 1002B was 133.6.degree.
F., the temperature in stage 1002C was 148.2.degree. F., the
temperature in stage 1002D was 158.6.degree. F., the temperature in
stage 1002E was 167.1.degree. F., the temperature in 1002F was
171.6.degree. F., the temperature in stage 1002G was 174.4.degree.
F., and the temperature in stage 1002H was 175.3.degree. F. Sump
volume 1002I, located at the bottom of condenser 1002, had 9.3
inches of water. The substantially pure water stream then exited
condenser 1002 through liquid outlet 1008 at a temperature of
175.4.degree. F.
As the substantially pure water stream exited condenser 1002, a
pump (not shown) operating at 72.7% capacity pumped the water
stream to heat exchanger 1004 at a volumetric flow rate of 191.0
gallons per minute. As the substantially pure water stream flowed
through heat exchanger 1004, heat was transferred from the
substantially pure water stream to another fluid stream flowing
through heat exchanger 1004, and the temperature of the
substantially pure water stream was reduced from 175.4.degree. F.
to 145.8.degree. F. After flowing through heat exchanger 1004 and
becoming chilled, a first portion of the chilled substantially pure
water stream was flowed through liquid conduit 1012 to a purified
water reservoir (not shown). A second portion of the chilled
substantially pure water stream was flowed through a cooling device
1024. In cooling device 104, the second portion of the chilled
substantially pure water stream was further chilled, and the
temperature of the second portion of the chilled substantially pure
water stream was further reduced to 120.degree. F. The further
chilled substantially pure water stream was then returned to
condenser 1002 via conduit 1010 through liquid inlet 1006.
In heat exchanger 1004, a salt-containing water stream was flowed
counterflow to the substantially pure water stream. Initially, the
salt-containing water stream flowed from a source of
salt-containing water through liquid conduit 1014. As it entered
heat exchanger 1004, the salt-containing water stream was at a
temperature of 133.8.degree. F. and a pressure of 48.7 psi. After
flowing through heat exchanger 1004 and receiving heat transferred
from the substantially pure water stream, the temperature of the
salt-containing water stream increased to 164.9.degree. F. The
pressure of the salt-containing water stream was 44.9 psi. The
heated salt-containing water stream was then flowed to the
humidifier.
Example 4
As shown in FIG. 11A, this example describes an HDH system 1100,
which comprises a humidifier 1102, a multi-stage bubble column
condenser 1104, an external heat exchanger 1106, an external
heating device 1108, and an external cooling device 1110.
In operation, a brine stream enters heat exchanger 1106, which is a
plate-and-frame heat exchanger, at a flow rate of 620 gallons per
minute (gpm) and a temperature of 130.degree. F. In heat exchanger
1106, heat is transferred from a hot fresh water stream exiting
condenser 1104 to the brine stream, and the temperature of the
brine stream is increased by 30.degree. F., from 130.degree. F. to
160.degree. F. This step advantageously recovers energy from the
hot fresh water stream and reduces the amount of heat required to
be supplied by heating device 1108.
The heated brine stream then flows through liquid conduit 1112 and
enters heating device 1108 at a flow rate of 625 gpm and a
temperature of 160.degree. F. As the heated brine stream flows
through heating device 1108, which is a plate-and-frame heat
exchanger, heat is transferred from a stream of hot, pressurized
water to the heated brine stream, resulting in the heated brine
stream being further heated to a temperature of 200.degree. F.
The further heated brine stream then flows through liquid conduit
1114 and enters humidifier 1102 at a flow rate of 632 gpm and a
temperature of 200.degree. F. As the further heated brine stream
flows in a first direction from a brine inlet located at a first
end (e.g., a top end) of humidifier 1102 to a brine outlet located
at a second end (e.g., a bottom end) of humidifier 1102, the brine
stream comes into direct contact with a stream of ambient air
flowing in a second, substantially opposite direction through
humidifier 1102. The stream of ambient air enters humidifier 1102
at a flow rate of 8,330 actual cubic feet per minute (acfm) and a
temperature of 60.degree. F. As the stream of ambient air flows in
the second direction through humidifier 1102, heat and mass are
transferred from the further heated brine stream to the ambient air
stream, resulting in a humidified air stream and a concentrated
brine stream. The concentrated brine stream exits humidifier 1102
at a flow rate of 593 gpm and a temperature of 135.degree. F. and
is subsequently discharged from HDH system 1100 via conduit
1116.
The humidified air stream exits humidifier 1102 through a main
humidifier air outlet and flows through gas conduit 1118 to
multi-stage bubble condenser 1104. The humidified air stream enters
condenser 1104 through a main condenser humidified air inlet at a
flow rate of 15,000 acfm and a temperature of 173.degree. F. In
condenser 1104, the humidified air stream comes into direct contact
with a fresh water stream, which enters condenser 1104 through a
condenser fresh water inlet at a flow rate of 550 gpm and a
temperature of 125.degree. F. In condenser 1104, heat and mass are
transferred from the humidified air stream to the fresh water
stream as water is condensed from the humidified air stream,
resulting in a dehumidified air stream and a heated fresh water
stream. The dehumidified air stream exits condenser 1104 through a
condenser air outlet at a flow rate of 9,500 acfm and a temperature
of 127.degree. F. The heated fresh water stream exits condenser
1104 through a condenser fresh water outlet at a flow rate of 575
gpm and a temperature of 170.degree. F. The heated fresh water
stream then flows through heat exchanger 1106, where heat is
transferred from the heated fresh water stream to the brine stream
entering HDH system 1100, resulting in a cooled fresh water stream
and the heated brine stream. After flowing through heat exchanger
1106, a first portion of the cooled fresh water stream exits HDH
system 1100 via a condenser condensate outlet at a flow rate of 25
gpm and a temperature of 140.degree. F. A second portion of the
fresh water stream flows to cooling device 1110, which is an
air-cooled heat exchanger. As the cooled fresh water stream flows
through cooling device 1110, heat is transferred from the cooled
fresh water stream to a stream of air, and the cooled fresh water
stream is further cooled to a temperature of 125.degree. F. The
further cooled fresh water stream then returns to condenser 1104
through a condenser fresh water inlet at a flow rate of 550 gpm and
a temperature of 125.degree. F.
Example 5
This example describes the HDH system 1100 of Example 3, with the
addition of an intermediate gas conduit 1122 connecting humidifier
1102 and condenser 1104. When this system, which is shown in FIG.
11B, is in operation, air is extracted from humidifier 1102 at an
intermediate air outlet. The air subsequently flows through
intermediate gas conduit 1122 and is injected directly into an
intermediate location in condenser 1104. The locations of the
extraction and injection points are selected in order to optimize
the thermal efficiency of the system. Because the intermediate air
stream is extracted from humidifier 1102 before the stream has
flowed through the entire humidifier, the temperature of the
intermediate air stream is lower than the temperature of the
humidified air stream exiting humidifier 1102 through a main
humidifier air outlet. For example, while the humidified air stream
exiting humidifier 1102 through the main air outlet enters
condenser 1104 at a flow rate of 12,000 acfm and a temperature of
173.degree. F., the intermediate air stream exiting humidifier 1102
through the intermediate air outlet enters condenser 1104 at a flow
rate of 8,000 acfm and a temperature of 160.degree. F.
Example 6
This example describes an HDH system 1100 comprising a humidifier
1102, a multi-stage bubble column condenser 1124 comprising an
internal heat exchanger, an external heating device 1108, and an
external cooling device 1110. This system is shown in FIG. 11C.
When HDH system 1100 is in operation, a brine stream enters the
internal heat exchanger of condenser 1124 at a flow rate of 620 gpm
and a temperature of 115.degree. F. As the brine stream flows
through the internal heat exchanger of condenser 1124, heat is
transferred to the brine stream from a fresh water stream flowing
through condenser 1124, resulting in a heated brine stream that
exits condenser 1124 at a flow rate of 625 gpm and a temperature of
160.degree. F. The heated brine stream then flows through liquid
conduit 1112 to heating device 1108, where the heated brine stream
is further heated to a temperature of 200.degree. F. The further
heated brine stream then flows through conduit 1114 and enters
humidifier 1102 at a flow rate of 632 gpm and a temperature of
200.degree. F.
In humidifier 1102, the further heated brine stream comes into
direct contact with an ambient air stream, which enters humidifier
1102 at a flow rate of 8,330 acfm and a temperature of 80.degree.
F. Heat and mass are transferred from the further heated brine
stream to the ambient air stream, resulting in a humidified air
stream and a concentrated brine stream. The concentrated brine
stream exits humidifier 1102 at a flow rate of 593 gpm and a
temperature of 135.degree. F. A first portion of the concentrated
brine stream exits HDH system 1100, and a second portion of the
concentrated brine stream flows to cooling device 1110, where the
concentrated brine stream is cooled to a temperature of 120.degree.
F. The cooled brine stream exits cooling device 1110 at a flow rate
of 593 gpm and a temperature of 120.degree. F. The cooled brine
stream is combined with a stream of incoming brine, which enters at
a flow rate of 25 gpm and a temperature of 60.degree. F., before
returning to condenser 1124 at a temperature of 115.degree. F.
The humidified air stream exits a main air outlet of humidifier
1102 and enters condenser 1124 at a flow rate of 15,000 acfm and a
temperature of 173.degree. F. In condenser 1124, the humidified air
stream comes into contact with the fresh water stream, and purified
water is condensed from the humidified air stream, resulting in a
dehumidified air stream. The purified water enters the fresh water
stream, which exits condenser 1124 at a flow rate of 25 gpm and a
temperature of 170.degree. F. The dehumidified air stream exits
condenser 1124 at a flow rate of 9500 acfm and a temperature of
127.degree. F.
Example 7
This example describes the HDH system 1100 of Example 5, with the
addition of an intermediate gas conduit 1122 connecting humidifier
1102 and condenser 1124. When this system, which is shown in FIG.
11D, is in operation, air is extracted from humidifier 1102 at an
intermediate air outlet. The air subsequently flows through
intermediate gas conduit 1122 and is injected directly into an
intermediate location in condenser 1124. The locations of the
extraction and injection points are selected in order to optimize
the thermal efficiency of the system. Because the intermediate air
stream is extracted from humidifier 1102 before the stream has
flowed through the entire humidifier, the temperature of the
intermediate air stream is lower than the temperature of the
humidified air stream exiting humidifier 1102 through a main
humidifier air outlet. For example, while the humidified air stream
exiting humidifier 1102 through the main air outlet enters
condenser 1124 at a flow rate of 12,000 acfm and a temperature of
173.degree. F., the intermediate air stream exiting humidifier 1102
through the intermediate air outlet enters condenser 1104 at a flow
rate of 8,000 acfm and a temperature of 160.degree. F.
Having thus described several aspects of some embodiments of this
invention, it is to be appreciated various alterations,
modifications, and improvements will readily occur to those skilled
in the art. Such alterations, modifications, and improvements are
intended to be part of this disclosure, and are intended to be
within the spirit and scope of the invention. Accordingly, the
foregoing description and drawings are by way of example only.
* * * * *
References